CA2033671C - Method of producing olefin polymer graft copolymers - Google Patents
Method of producing olefin polymer graft copolymersInfo
- Publication number
- CA2033671C CA2033671C CA002033671A CA2033671A CA2033671C CA 2033671 C CA2033671 C CA 2033671C CA 002033671 A CA002033671 A CA 002033671A CA 2033671 A CA2033671 A CA 2033671A CA 2033671 C CA2033671 C CA 2033671C
- Authority
- CA
- Canada
- Prior art keywords
- monomer
- olefin polymer
- polymer material
- pph
- weight
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000000034 method Methods 0.000 title claims abstract description 74
- 229920000098 polyolefin Polymers 0.000 title claims abstract description 62
- 229920000578 graft copolymer Polymers 0.000 title claims abstract description 23
- 239000000178 monomer Substances 0.000 claims abstract description 130
- 239000003999 initiator Substances 0.000 claims abstract description 58
- 150000003254 radicals Chemical class 0.000 claims abstract description 30
- 230000001590 oxidative effect Effects 0.000 claims abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 claims abstract description 5
- 239000007870 radical polymerization initiator Substances 0.000 claims abstract description 4
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Natural products C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 85
- -1 unsaturated aliphatic nitriles Chemical class 0.000 claims description 59
- 239000002861 polymer material Substances 0.000 claims description 50
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 28
- 239000005977 Ethylene Substances 0.000 claims description 26
- 229920001155 polypropylene Polymers 0.000 claims description 20
- 239000000203 mixture Substances 0.000 claims description 16
- 229920001577 copolymer Polymers 0.000 claims description 15
- 229920001519 homopolymer Polymers 0.000 claims description 15
- 238000000354 decomposition reaction Methods 0.000 claims description 14
- 239000011148 porous material Substances 0.000 claims description 14
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims description 13
- 229920001384 propylene homopolymer Polymers 0.000 claims description 13
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 12
- 229920001971 elastomer Polymers 0.000 claims description 11
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 10
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 claims description 7
- CQEYYJKEWSMYFG-UHFFFAOYSA-N butyl acrylate Chemical compound CCCCOC(=O)C=C CQEYYJKEWSMYFG-UHFFFAOYSA-N 0.000 claims description 7
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 claims description 6
- 150000002148 esters Chemical class 0.000 claims description 6
- 229920005604 random copolymer Polymers 0.000 claims description 6
- 150000001993 dienes Chemical class 0.000 claims description 5
- 229920000181 Ethylene propylene rubber Polymers 0.000 claims description 4
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 claims description 4
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 4
- 125000003118 aryl group Chemical group 0.000 claims description 4
- HQQADJVZYDDRJT-UHFFFAOYSA-N ethene;prop-1-ene Chemical group C=C.CC=C HQQADJVZYDDRJT-UHFFFAOYSA-N 0.000 claims description 4
- 229920001038 ethylene copolymer Polymers 0.000 claims description 4
- 150000002894 organic compounds Chemical class 0.000 claims description 4
- 229920001897 terpolymer Polymers 0.000 claims description 4
- GOXQRTZXKQZDDN-UHFFFAOYSA-N 2-Ethylhexyl acrylate Chemical compound CCCCC(CC)COC(=O)C=C GOXQRTZXKQZDDN-UHFFFAOYSA-N 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 239000004711 α-olefin Substances 0.000 claims description 3
- 150000001334 alicyclic compounds Chemical class 0.000 claims description 2
- 150000001491 aromatic compounds Chemical class 0.000 claims description 2
- 150000002391 heterocyclic compounds Chemical class 0.000 claims description 2
- 229920001567 vinyl ester resin Polymers 0.000 claims description 2
- 125000003011 styrenyl group Chemical group [H]\C(*)=C(/[H])C1=C([H])C([H])=C([H])C([H])=C1[H] 0.000 claims 5
- 125000005395 methacrylic acid group Chemical class 0.000 claims 3
- 150000007933 aliphatic carboxylic acids Chemical class 0.000 claims 2
- 150000003440 styrenes Chemical class 0.000 claims 2
- 239000000463 material Substances 0.000 claims 1
- MMCOUVMKNAHQOY-UHFFFAOYSA-L oxido carbonate Chemical compound [O-]OC([O-])=O MMCOUVMKNAHQOY-UHFFFAOYSA-L 0.000 claims 1
- 229920006395 saturated elastomer Polymers 0.000 claims 1
- 150000002978 peroxides Chemical class 0.000 abstract description 9
- 230000008569 process Effects 0.000 abstract description 9
- 229920002554 vinyl polymer Polymers 0.000 abstract description 5
- 238000012667 polymer degradation Methods 0.000 abstract 1
- 238000007792 addition Methods 0.000 description 68
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 38
- 238000006243 chemical reaction Methods 0.000 description 31
- 229920000642 polymer Polymers 0.000 description 23
- 229910052757 nitrogen Inorganic materials 0.000 description 19
- 239000004743 Polypropylene Substances 0.000 description 18
- 240000001987 Pyrus communis Species 0.000 description 18
- 239000002245 particle Substances 0.000 description 18
- 239000004615 ingredient Substances 0.000 description 17
- 150000001336 alkenes Chemical class 0.000 description 13
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 10
- 238000010926 purge Methods 0.000 description 9
- 239000002904 solvent Substances 0.000 description 9
- 239000007788 liquid Substances 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 7
- 239000003085 diluting agent Substances 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- WSSSPWUEQFSQQG-UHFFFAOYSA-N 4-methyl-1-pentene Chemical compound CC(C)CC=C WSSSPWUEQFSQQG-UHFFFAOYSA-N 0.000 description 4
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 4
- 230000015556 catabolic process Effects 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000010559 graft polymerization reaction Methods 0.000 description 4
- 229920001903 high density polyethylene Polymers 0.000 description 4
- 239000004700 high-density polyethylene Substances 0.000 description 4
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 230000000379 polymerizing effect Effects 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000004793 Polystyrene Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- ZFTFAPZRGNKQPU-UHFFFAOYSA-N dicarbonic acid Chemical compound OC(=O)OC(O)=O ZFTFAPZRGNKQPU-UHFFFAOYSA-N 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 229920000092 linear low density polyethylene Polymers 0.000 description 3
- 239000004707 linear low-density polyethylene Substances 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 229920002223 polystyrene Polymers 0.000 description 3
- WYKYCHHWIJXDAO-UHFFFAOYSA-N tert-butyl 2-ethylhexaneperoxoate Chemical compound CCCCC(CC)C(=O)OOC(C)(C)C WYKYCHHWIJXDAO-UHFFFAOYSA-N 0.000 description 3
- GJBRNHKUVLOCEB-UHFFFAOYSA-N tert-butyl benzenecarboperoxoate Chemical group CC(C)(C)OOC(=O)C1=CC=CC=C1 GJBRNHKUVLOCEB-UHFFFAOYSA-N 0.000 description 3
- OZAIFHULBGXAKX-UHFFFAOYSA-N 2-(2-cyanopropan-2-yldiazenyl)-2-methylpropanenitrile Chemical compound N#CC(C)(C)N=NC(C)(C)C#N OZAIFHULBGXAKX-UHFFFAOYSA-N 0.000 description 2
- NGFUZFAPKBLICJ-UHFFFAOYSA-N 2-but-1-enylpyridine Chemical compound CCC=CC1=CC=CC=N1 NGFUZFAPKBLICJ-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 125000001931 aliphatic group Chemical group 0.000 description 2
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 description 2
- 125000003236 benzoyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C(*)=O 0.000 description 2
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 2
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 2
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000006193 liquid solution Substances 0.000 description 2
- 229920001684 low density polyethylene Polymers 0.000 description 2
- 239000004702 low-density polyethylene Substances 0.000 description 2
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 238000002459 porosimetry Methods 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 2
- HGTUJZTUQFXBIH-UHFFFAOYSA-N (2,3-dimethyl-3-phenylbutan-2-yl)benzene Chemical group C=1C=CC=CC=1C(C)(C)C(C)(C)C1=CC=CC=C1 HGTUJZTUQFXBIH-UHFFFAOYSA-N 0.000 description 1
- HGXJDMCMYLEZMJ-UHFFFAOYSA-N (2-methylpropan-2-yl)oxy 2,2-dimethylpropaneperoxoate Chemical compound CC(C)(C)OOOC(=O)C(C)(C)C HGXJDMCMYLEZMJ-UHFFFAOYSA-N 0.000 description 1
- NOBYOEQUFMGXBP-UHFFFAOYSA-N (4-tert-butylcyclohexyl) (4-tert-butylcyclohexyl)oxycarbonyloxy carbonate Chemical compound C1CC(C(C)(C)C)CCC1OC(=O)OOC(=O)OC1CCC(C(C)(C)C)CC1 NOBYOEQUFMGXBP-UHFFFAOYSA-N 0.000 description 1
- HIDBROSJWZYGSZ-UHFFFAOYSA-N 1-phenylpyrrole-2,5-dione Chemical compound O=C1C=CC(=O)N1C1=CC=CC=C1 HIDBROSJWZYGSZ-UHFFFAOYSA-N 0.000 description 1
- QEDJMOONZLUIMC-UHFFFAOYSA-N 1-tert-butyl-4-ethenylbenzene Chemical compound CC(C)(C)C1=CC=C(C=C)C=C1 QEDJMOONZLUIMC-UHFFFAOYSA-N 0.000 description 1
- IGGDKDTUCAWDAN-UHFFFAOYSA-N 1-vinylnaphthalene Chemical compound C1=CC=C2C(C=C)=CC=CC2=C1 IGGDKDTUCAWDAN-UHFFFAOYSA-N 0.000 description 1
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- GLVYLTSKTCWWJR-UHFFFAOYSA-N 2-carbonoperoxoylbenzoic acid Chemical compound OOC(=O)C1=CC=CC=C1C(O)=O GLVYLTSKTCWWJR-UHFFFAOYSA-N 0.000 description 1
- VCWDAHMQCOZVQD-UHFFFAOYSA-N 2-chloroprop-1-enylbenzene Chemical compound CC(Cl)=CC1=CC=CC=C1 VCWDAHMQCOZVQD-UHFFFAOYSA-N 0.000 description 1
- WROUWQQRXUBECT-UHFFFAOYSA-N 2-ethylacrylic acid Chemical compound CCC(=C)C(O)=O WROUWQQRXUBECT-UHFFFAOYSA-N 0.000 description 1
- SMTDFMMXJHYDDE-UHFFFAOYSA-N 2-prop-1-enylpyridine Chemical compound CC=CC1=CC=CC=N1 SMTDFMMXJHYDDE-UHFFFAOYSA-N 0.000 description 1
- KGIGUEBEKRSTEW-UHFFFAOYSA-N 2-vinylpyridine Chemical compound C=CC1=CC=CC=N1 KGIGUEBEKRSTEW-UHFFFAOYSA-N 0.000 description 1
- GNSFRPWPOGYVLO-UHFFFAOYSA-N 3-hydroxypropyl 2-methylprop-2-enoate Chemical class CC(=C)C(=O)OCCCO GNSFRPWPOGYVLO-UHFFFAOYSA-N 0.000 description 1
- YHQXBTXEYZIYOV-UHFFFAOYSA-N 3-methylbut-1-ene Chemical compound CC(C)C=C YHQXBTXEYZIYOV-UHFFFAOYSA-N 0.000 description 1
- RITONZMLZWYPHW-UHFFFAOYSA-N 3-methylhex-1-ene Chemical compound CCCC(C)C=C RITONZMLZWYPHW-UHFFFAOYSA-N 0.000 description 1
- LDTAOIUHUHHCMU-UHFFFAOYSA-N 3-methylpent-1-ene Chemical compound CCC(C)C=C LDTAOIUHUHHCMU-UHFFFAOYSA-N 0.000 description 1
- JLBJTVDPSNHSKJ-UHFFFAOYSA-N 4-Methylstyrene Chemical compound CC1=CC=C(C=C)C=C1 JLBJTVDPSNHSKJ-UHFFFAOYSA-N 0.000 description 1
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 1
- GAWIXWVDTYZWAW-UHFFFAOYSA-N C[CH]O Chemical group C[CH]O GAWIXWVDTYZWAW-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-M Methacrylate Chemical compound CC(=C)C([O-])=O CERQOIWHTDAKMF-UHFFFAOYSA-M 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 description 1
- GYCMBHHDWRMZGG-UHFFFAOYSA-N Methylacrylonitrile Chemical compound CC(=C)C#N GYCMBHHDWRMZGG-UHFFFAOYSA-N 0.000 description 1
- WHNWPMSKXPGLAX-UHFFFAOYSA-N N-Vinyl-2-pyrrolidone Chemical compound C=CN1CCCC1=O WHNWPMSKXPGLAX-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 150000001252 acrylic acid derivatives Chemical class 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 125000002723 alicyclic group Chemical group 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 125000003710 aryl alkyl group Chemical group 0.000 description 1
- 229920005601 base polymer Polymers 0.000 description 1
- WURBFLDFSFBTLW-UHFFFAOYSA-N benzil Chemical group C=1C=CC=CC=1C(=O)C(=O)C1=CC=CC=C1 WURBFLDFSFBTLW-UHFFFAOYSA-N 0.000 description 1
- 125000001797 benzyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])* 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000007334 copolymerization reaction Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 229940057404 di-(4-tert-butylcyclohexyl)peroxydicarbonate Drugs 0.000 description 1
- LSXWFXONGKSEMY-UHFFFAOYSA-N di-tert-butyl peroxide Chemical compound CC(C)(C)OOC(C)(C)C LSXWFXONGKSEMY-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- XJELOQYISYPGDX-UHFFFAOYSA-N ethenyl 2-chloroacetate Chemical compound ClCC(=O)OC=C XJELOQYISYPGDX-UHFFFAOYSA-N 0.000 description 1
- ANTNQGGUTAZUIC-UHFFFAOYSA-N ethenyl 2-cyanoacetate Chemical compound C=COC(=O)CC#N ANTNQGGUTAZUIC-UHFFFAOYSA-N 0.000 description 1
- GFJVXXWOPWLRNU-UHFFFAOYSA-N ethenyl formate Chemical compound C=COC=O GFJVXXWOPWLRNU-UHFFFAOYSA-N 0.000 description 1
- UIWXSTHGICQLQT-UHFFFAOYSA-N ethenyl propanoate Chemical compound CCC(=O)OC=C UIWXSTHGICQLQT-UHFFFAOYSA-N 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 125000001475 halogen functional group Chemical group 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 125000000623 heterocyclic group Chemical group 0.000 description 1
- 239000012456 homogeneous solution Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 150000002734 metacrylic acid derivatives Chemical class 0.000 description 1
- FQPSGWSUVKBHSU-UHFFFAOYSA-N methacrylamide Chemical compound CC(=C)C(N)=O FQPSGWSUVKBHSU-UHFFFAOYSA-N 0.000 description 1
- 229940063557 methacrylate Drugs 0.000 description 1
- ZGEGCLOFRBLKSE-UHFFFAOYSA-N methylene hexane Natural products CCCCCC=C ZGEGCLOFRBLKSE-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 125000002950 monocyclic group Chemical group 0.000 description 1
- 125000004108 n-butyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- KKFHAJHLJHVUDM-UHFFFAOYSA-N n-vinylcarbazole Chemical compound C1=CC=C2N(C=C)C3=CC=CC=C3C2=C1 KKFHAJHLJHVUDM-UHFFFAOYSA-N 0.000 description 1
- 150000001451 organic peroxides Chemical class 0.000 description 1
- 239000011236 particulate material Substances 0.000 description 1
- 125000000286 phenylethyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])([H])C([H])([H])* 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000003505 polymerization initiator Substances 0.000 description 1
- 229920005606 polypropylene copolymer Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000003252 repetitive effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000006561 solvent free reaction Methods 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 125000001424 substituent group Chemical group 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- PHYFQTYBJUILEZ-IUPFWZBJSA-N triolein Chemical compound CCCCCCCC\C=C/CCCCCCCC(=O)OCC(OC(=O)CCCCCCC\C=C/CCCCCCCC)COC(=O)CCCCCCC\C=C/CCCCCCCC PHYFQTYBJUILEZ-IUPFWZBJSA-N 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- KOZCZZVUFDCZGG-UHFFFAOYSA-N vinyl benzoate Chemical compound C=COC(=O)C1=CC=CC=C1 KOZCZZVUFDCZGG-UHFFFAOYSA-N 0.000 description 1
- ORGHESHFQPYLAO-UHFFFAOYSA-N vinyl radical Chemical compound C=[CH] ORGHESHFQPYLAO-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F255/00—Macromolecular compounds obtained by polymerising monomers on to polymers of hydrocarbons as defined in group C08F10/00
-
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Abstract
Disclosed is a method of making graft copolymers of olefin polymers by contacting a particulate olefin polymer with a free radical polymerization initiator, e.g., a peroxide, and a vinyl monomer at about from 60° to 125° C
while controlling the monomer addition rate so that it does not exceed about 4.5 pph/min, and most preferably does not exceed about 3.0 pph/min, at any monomer feed level. To prevent polymer degradation, a non-oxidizing environment is maintained throughout the process, and residual free radicals are deactivated, and unreacted initiator is decomposed, before the graft copolymer is exposed to all.
while controlling the monomer addition rate so that it does not exceed about 4.5 pph/min, and most preferably does not exceed about 3.0 pph/min, at any monomer feed level. To prevent polymer degradation, a non-oxidizing environment is maintained throughout the process, and residual free radicals are deactivated, and unreacted initiator is decomposed, before the graft copolymer is exposed to all.
Description
20~3671 2291s Case 7001 + 7001-2 The present invention relates to a method of making graft copolymers of polyolefins, and, more particularly, to a method of graft polymerizing monomers at free radical sites produced on olefin polymer backbones by chemical free radical initiators of polymerization.
Graft copolymers of polypropylene have been of interest for some time because they are capable of possessing some properties o~ the grated polymer (produced by the homo- or copolymerization of the monomer or monomers, respectively) as well as of the polypropylene backbone. It has been suggested, for e~ample, that some o~
these graft copolymers be used as compatibilizers for normally immiscible polymer systems and as components o~
gum plastic compositions.
The preparation of graft copolymers by creating acti~e sites on the main polymer chain or backbone, and initiatirlq graft polymerization of a polymerizable monomer at these sites, is well-known. Procedures which have been used or introducing such active sites into the polymer chain have included treatment with organic chemical compounds capable of generating free radicals, and irradiation. In the chémical method, àn organic chemical compound capable o~
generating free radicals, such as a peroxide or azo compound, is decomposed in the presence of the backbone polymer with the formation of free radicals, which form ~e active grafting sites on the polymer and initiate the polymeriz~tion of the monomer at these sites.
Of the various techniques which have been employed for preparing gra~t copolymers o~ polyolefins by the chemic~l method of free radical generation, the bulk technique, i~
which the polymer particles are contacted directly with 20:~3671 , initiator and monomer, without the intervention of a liquid suspending medium or a solvent, is advantageous in terms of simplicity of execution and the avoidance of side-reactions caused by the presence of certain solvents or suspending media, such as water. However, regardless of the physical state of the polymer to be grafted, the grafting process is subject to problems such as degradation of the polyolefin, possibly leading to a graft copolymer having an undesirably high melt flow rate, and excessive formation of the homopolymer of the grafting monomer at the expense of the formation of the polyolefin graft copolymer.
U.S. Patent 4,595,726 discloses graft copolymers of 3-100%, preferably 3-30%, by weight of an alkyl meth-acrylate moiety grafted onto a polypropylene backbone. The lS graft copolymers, useful as adhesives in polypropylene laminates, are prepared at a temperature below the softening point of polypropylene by a solvent-free reaction, reportedly vapor-phase, between polypropylene an~
the methacrylate monomer in the presence of a free-radical-forming catalyst. A preferred initiator is tert-butyl perbenzoate, stated as having a 15-minute half-life at 135 C, and reactor temperatures of 135C and 140C are disclosed. Degradation of the polypropylene chain due to the reaction conditions employed is reported. Immediately after the pero~ide is added to the polypropylene, the monomer is added over a time period which is fi~ed by the half-life of the pero~ide initiator (i.e., 1-2 half-lives) In other words, according to the teachings of U.S. Patent 4,595,726, for a given initiator half-life, it is necessd~y to employ a higher rate of addition of the monomer as the total amount of monomer to be added increases.
The preparation of "graft-type copolymers by dissolving an organic pero~ide in a monomer and adding th~
solution to free-flowing particles of the base polymer, particularly polyvinyl chloride, is described in U.S.
Patent 3,240,843. The "graft-type" products are described as having monomeric, as opposed to polymeric, branches attached to the polymer backbone. Homopolymerization of the monomer also is mentioned. To avoid particle agglomeration, the amount of monomer added cannot exceed the maximum absorbable by the polymer particles. In the case of polypropylene charged into a reactor with a solution containing styrene, butadiene, acrylonitrile, and benzoyl pero~ide, the total amount of monomers added is only 9% of the amount of polypropylene charged.
The present invention provides a method of making an olefin polymer graft copolymer wherein free radical sites are produced in a particulate olefin polymer material by treating the polymer material at a temperature of about from 60 to 125C with about from 0.1 to 6.0 pph (parts by weight per 100 parts by weight of the olefin polymer material) of an organic chemical compound which is a free radical polymerization initiator and has a decomposition half-life of about from 1 to 240 minutes at the temperature employed.
Over a time period which coincides with, or follows, the period of initiator treatment, with or without overlap the polymer material is treated with about from S to 240 pph of a grafting monomer which is capable of being polymerized by free radicals, the temperature employed during any period of monomer treatment being as indicated above with respect to initiator treatment. The addition of the grafting monomer to the polymer material is controlled so that at all addition levels of about from 5 to 240 pph the rate of addition does not e~ceed about 4.5, pre~erably does not e~ceed about 4.0, and most preferably does not e~ceed about 3.0, pph per minute.
After the grafting period, i.e., the period o~
treatment with the grafting monomer, and any hold period at reaction conditions subsequent thereto, any unreacted monomer is removed from the resultant grafted particulate olefin polymer material, and the decomposition o~ any unreacted initiator and deactivation of any residual free radicals are promoted, e.g., by a temperature increase.
During the entire process the polymer material is maintained in a substantially non-oxidizing environment.
The method of this invention embodies a combination of steps which together permit olefin polymer graft copolymers to be obtained not only in high conversions (monomer consumption) but also with a high degree of graft efficiency. Moreover, degradation of the backbone olefin polymer is minimized, thereby avoiding the production of a graft copolymer having a melt flow rate which is sub-stantially higher than that of the starting backbone olefin polymer, a condition that can adversely afect the processing behavior of the graft copolymer.
While not wishing to be bound or limited in any way by theoretical considerations, we believe that the high degree of eficiency afforded by the method of the invention is related to the manner in which the grafting monomer is brought into contact with the olefin polymer particles in which free radical sites have been, and/or are being, produced by contact of the initiator with the heated particles. The low rate of addition of the monomer, i.e., a rate not e~ceeding about 4.5, preferably no greater than about 4.0, and most preferably no greater than about 3.0, pph per minute, creates an essentially ~dryn condition in which the monomer liquid and the initiator come together in the presenCe of heat (i.e., that needed to decompose the initiator) instead of in a large volume of monomer liquid.
It has been found that homopolymerization of the monomer, at the e~pense of a graft polymerization reaction, becomes more prevalent at rates of monomer addition which resul~ ~n a buildup of monomer liquid within and between polymer particles. It is believed that, in the latter case, the ;
so-called "wet" condition due to the buildup of ~o~m~
liquid may facilitate or promote the sel-polymerization of the monomer rather than graft polymerization with the olefin polymer particles.
In the present process, the monomer feed rate can be as low as desired, and the minimum generally will be dictated by the capability of available equipment and economic considerations. While rates of at least about 0.1 - 0.2 pph/min can be used, a preferred practical minimum is about 0.3 pph/min. Preferred rates in any particular case will depend on such factors as the monomer feed level, the initiator/monomer addition mode, and the reactivity of the particular monomer used.
The addition of monomer at a rate of about from 0.1 to 4.5 pph/min, preferably about from 0.3 to 4.0 pph/min and most preferably 0.3 to 3.0 pph/min results in high graft efficiencies with high monomer conversions over a wide range of monomer feed levels. The monomer addition rates set forth above, including those above the preferred ma~imum, are suitable with lower monomer feed levels, e.g., levels of up to about 40 pph. Also, a maximum monomer addition rate of about 4.0 pph/min is preferred provided that the monomer feed level does not exceed about 40 pph.
With feed levels above about 40 pph, addition rates of about 0.3 to about 3.0 pph/min are used to provide high graft efficiencies. Such rates are most preferred in the present process because of their applicability over a wider range of monomer feed levels. With the most preferred monomer addition rates, and especially at rates up to abo~t 3.0 pph~min, high graft efficiencies are attained at hi~h monomer conversions regardless of addition mode even at high monomer feed levels of 100 pph and above.
The above-specified monomer addition rate must be adhered to at all addition levels of monomer to be adde~, i.e., addition levels of about from 5 to 240 pph, and is ~f 20:~3571 increasingly qreater importance at higher addition levels.
In contrast, the fixed addition time advocated by the aforementioned U.S. Patent 4,595,726 results in the use of the highest monomer addition rates at the highest addition levels, i.e., the very levels at which, according to the present invention, low addition rates are most important.
A fixed addition time, e.g., 1-2 half-lives of an initiator such as tert-butyl perbenzoate, as taught in the afore-mentioned patent, will not be long enough to result in a sufficiently low addition rate at the large monomer additions needed to produce high graft levels with a hiyh degree of efficiency.
In one embodiment of the present method, the time period during which the mass of olefin polymer particles is treated with the grafting monomer follows the time period during which the particle mass is treated with the initiator. In this case (separate-addition mode), the initiator is added first to the particles, which are preferably heated to the temperature being used, and the production of free radical sites in the olefin polymer material begins. The addition of the monomer may begin immediately after the addition of the initiator has been completed, or after a delay or hold time subsequent to the completion of the initiator addition. Separate additions also can be multi-staged whereby the additions are incre-mental and the initiator/monomer addition sequence is repetitive. In another embodiment, the initiator and the monomer are added to the heated polymer particles at the same time (côncurrent-addition mode), e.g., by combininq the initiator (neat or a liquid solution thereof) and the monomer (neat or a liquid solution thereof~ at a temper-ature at which no appreciable decomposition of the initiator occurs. The concurrent addition of separate initiator and monomer streams also can be employed, as ~ell as a combination of separate addition and concurrent 20336~1 ._ addition, in which the monomer addition period follows the initiator addition period with overlap. Whether the initiator and monomer are added concurrently or monomer addition follows initiator addition, either the initiator S or monomer, or both, can be added continuously or intermittently. The method of the invention can be carried out as a semi-batch, semi-continuous, or continuous process.
In the present process the particulate olefin polymer material which is treated with the initiator and the grafting monomer is at a temperature of about from 60 to 125C, preferably about from 80 to 120C. While temperatures below about 60C can be used, the decomposi-tion half-life of many free radical initiators at such temperatures is so long as to be impractical, and initiators having a short enough half-life below about 60C
often are difficult to handle. Above about 125C, the sharp reduction in decomposition half-life which occurs with many initiators causes the monomer conversion to dro~, especially in the separate-addition mode. Moreover, initiators having longer half-lives at temperatures abo~e about 125C tend to have an adverse effect on the ole~in polymer and/or the resulting graft copolymer.
Treating the olefin polymer material with the initiator and the monomer at a temperature as set forth above provides an initiator half-life of about from 1 to 240 minutes. After the addition of the monomer, the thus-treated polymer material may be maintained at the selected temperature for at least about 3, and most preferably at least about 10, minutes. This hold period may be e~tended to several hours, especially at lower temperatures. Preferably the initiator and temperature will be selected to allow grafting to be completed within about 2 to 10 initiator half-lives. Conditions that ~e~ul~
in half-lives below about 2 minutes are not preferred, especially in the separate-addition mode with delayed 2~33671 .
monomer addition, inasmuch as the conversion may be deleteriously affected if the initiator is allowed to decompose rapidly before the monomer addition begins.
To assure a high conversion and graft efficiency, and effective use of the initiator, a time of at least about 1, preferably at least about 2, initiator half-lives at the selected temperature should elapse between the start of the initiator addition period and the end of the monomer removal step. The time from the start of monomer addition to the end of the grafting period depends on the amount of monomer used and the rate of addition, longer times being used at lower temperatures and higher monomer feed levels.
At the monomer addition rates used in the present process, the hold period, if any, after completion of the monomer addition generally is as stated above, longer hold periods after monomer addition preferably being used at lower temperatures and higher monomer feed levels. In the separate-addition mode, preferably no more than about 2.5 initiator half-lives should separate the initiator and monomer addition periods to assure the availability of ttle necessary free radicals once the addition of the monomer begins.
The olefin polymer material useful in the practice o~
the method of this invention for making graft copolymers of olefin polymers is (a) a homopolymer of a linear or branched C l-olefin; (b) a random copolymer of a linear or branched C2 8 l-olefin with a different olefin selected from the group consisting of C2 10 l-olefins, provided that, when the different olefin is ethylene, the ma~imum polymerized ethylene content is about 10~, prefer-ably about 4%, by weight; when the olefin is propylene and the different olefin is a C4 10 l-olefin, the maximum polymerized content thereof is about 20~, preferably abo~t 16%, by weight; and when the olefin is ethylene and the different olefin is a C3 10 l-ole~in, the maximum poly-merized content thereof is about 10%, preferably about 5%,by weiQht; (c) a random terpolymer of a linear or branched C3 8 l-olefin and two different olefins selected from the group consisting of ethylene and C4 8 l-olefins, provided that the maximum polymerized content o~ the different C4 8 l-olefins is about 20%, preferably about 16%, by weight, and, when ethylene is one of the different olefins, the ma~imum polymerized ethylene content is about 5%, preferably about 4%, by weight; or (d) a homopolymer of (a) or a random copolymer of (b) which is impact-modified with about from 10 to 60% of (i) an ethylene-propylene rubber having an ethylene content of about from 7 to 70%, preferably about from 7 to 40~, most preferably about from 10 to 40%, (ii) an ethylene/butene-l copolymer rubber (E~
having an ethylene content of from 30 to 70%, (iii) a propylene/butene-l copolymer rubber (PBR) having a butene-l content of from 30 to 70%, (iv) an ethylene-propylene-non-conjugated diene monomer rubber (EPDM) having an ethylene content of 30 to 70% and diene content of from 1 to 10%, (v) an ethylene/propylene/butene terpolymer rubber (~PBR) having a propylene content of from 1 to 10% and butene content of from 30 to 70% or a propylene content of from 30 to 70% and butene content of from 1 to 10%.
The C2 8 l-olefins which can be used in the preparation of the olefin polymer materials as described above include, for example, ethylene, propylene, l-butene, isobutylene, 3-methyl-1-butene, 3,4-dimethyl-1-butene, l-pentene, 4-methyl-1-pentene, l-hexene, 3-methyl-1-hexene l-heptene and the like. Propylene and l-butene are the preferred C3-C8 l-olefin monomers.
C3 10 l-olefins which can be used in the preparation of the olefin polymer materials as described above include linear and branched olefins such as those listed above ~or the C2 8 l-olefins which have at least 3 carbon atoms.
When the olefin polymer is an ethylene homopolymer, it has a density of 0.91 g/cm3 or greater, and when the olefin polymer is an ethylene copolymer with a C3 10 alpha-olefin, it has a density of 0.91 g/cm3 or greater.
Suitable ethylene copolymers include ethylene/butene-l, ethylene/hexene-l and ethylene/4-methyl-1-pentene. The ethylene copolymer can be a HDPE or a LLDPE, and the ethylene homopolymer can be a HDPE or a LDPE. Typically the LLDPE and LDPE have densities of 0.91 g/cm3 or greater and the HDPE have densities of 0.95 g/cm3 or greater.
The impact-modified olefin polymer can be prepared by first polymerizing a C2 8 l-olefin to form a homopolymer of said olefin, or copolymerizing such an olefin with a different olefin selected from C2 10 l-olefins, and then polymerizing the relevant monomers to form the rubber in the presence of said homopolymer or copolymer in a reactor or series of reactors. Alternatively, mechanical blends can be prepared by separately polymerizing 1) the parti-cular olefin to form the homo- or copolymer and 2) the relevant monomers to form the rubber, and then physically mixing the homo- or copolymer with the rubber until a homogeneous blend is obtained. Reactor blends are preferred when an impact-modified olefin polymer is used.
Homopolymers of butene-l, HDPE and LLDPE are preferred. Homopolymers, random copolymers, random terpolymers, and impact-modified homopolymers and copolymers of propylene are also preferred and are the most preferred olefin polymer materials for use in the present process and are referred to herein, individually or collectively, as propylene polymer materials.
Suitable particulate forms of the olefin polymer material used in the present method include powder, 1ak~, granulate, spherical, cubic and the like. Spherical particulate forms are preerred. The pore volume raction _ of the particles can be as low as about 0.04, but it is preferred that the grafting be effected on olefin polymer particles having a pore volume fraction o~ at least 0.07.
Most preferably, the olefin polymer used in the present method will have a pore volume fraction of at least about 0.12, and most preferably at least about 0.20, with more than 40%, preferably more than 50%, and most preferably more than 90%, of the pores having a diameter larger than 1 micron, a surface area of at least 0.1 m /g, and a weight averagè diameter of about from 0.4 to 7 mm. In the preferred polymer, grafting takes place in the interior o~
the particulate material as well as on the external surfaoe thereof, resulting in a substantially uniform distribution of the graft polymer throughout the ole~in polymer particle.
According to the method of the invention, free radical or active sites are produced in the particulate olefin polymer material by treating the polymer material with an organic compound which is a free-radical-generating polymerization initiator and has a decomposition half~
at the temperature employed o~ about from 1 to 240, preferably about from 5 to 100, and most preferably about from 10 to 40, minutes. Organic peroxides, and especially those which generate alkoxy radicals, constitute the preferred class of initiators. These include acyl peroxides, such as benzoyl and dibenzoyl pero~ides; dialkyl and aralkyl pero~ides, such as di-tert-butyl peroxide, dicumyl peroside, cumyl butyl pero~ide, l,l-di-tert-butylpero~y-3,5,5-trimethylcyclohexane, 2,5-dimethyl-2,5-di-tert-butylpero~yhexane, and bis(alpha-tert-butyl pero~yisopropylbenzene); pero~y esters, such as tert-butyl-pero~ypivalate, tert-butyl perbenzoate, 2,5-dimethylhexyl 2,5-di(perbenzoate), tert-butyl di(perphthalate), tert-butylpero~y-2-ethyl he~anoate; and 1,1-dimethyl-3-hydro~y-butylpero~y-2-ethyl hexanoate; and pero~y carbonates, such as di(2-ethylhe~yl) pero~y dicarbonate, di(n-propyl)per~y dicarbonate, and di(4-tert-butylcyclohexyl)peroxy dicar-bonate. Azo compounds, such as azobisisobutyronitrile, also may be used. Two or more initiators having the same or di~ferent half-lives may be employed.
The initiator, if a liquid at the decomposition temperature used, may be used neat or in solution. I~ a solid at the decomposition temperature used, it may be dissolved in a suitable liquid solvent. The concentration of the initiator in solution typically should be about ~rom 5% to g8% by weight. Peroxide initiators are available in hydrocarbon solutions at a concentration of about ~rom 12.5 to 75 weight %. Whether neat or in solution, the activ~
concentration of the initiator Der se should be about ~rom 0.1 to 6.0 pph, preferably about from 0.2 to 3.0 pph, to assure the generation of a sufficient number of free radical sites on and in the olefin polymer material.
The grafting monomers useful in accordance with this invention may be any monomeric vinyl compound capable o~
being polymerized by ~ree radicals wherein the vinyl radical, H2C~CR-, in which R , H or methyl, is attached to a straight or branched aliphatic chain or to a substituted or unsubstituted aromatic, heterocyclic, or alicyclic ring in a mono- or polycyclic compound. Typical substituent groups may be alkyl, hydro~yalkyl, aryl, and halo. Usually the vinyl monomer will be a member of one of the following classes: (1) vinyl-substituted aromatic, heterocyclic, or alicyclic compounds, including styrene, vinylnaphthalene, vinylpyridine, vinylpyrrolidone, vinylcarbazole, and homologs thereof, e.g., alpha- and para-methylstyrene, methylchlorostyrene, p-tert-butyl-styrene, methylvinylpyridine, and ethylvinylpyridine; (2) vinyl esters of aromatic and saturated aliphatic carboxYItC
acids, including vinyl formate, vinyl acetate, vinyl chloracetate, vinyl cyanoacetate, vinyl propionate, and vinyl benzoate; and (3) unsaturated aliphatic nitri les an4 carboxylic acids and their derivatives, including acry-lonitrile, methacrylonitrile, acrylamide, methacrylamide, acrylic acid, acrylate esters, such as the methyl, ethyl, hydroxyethyl, 2-ethylhexyl, and butyl acrylate esters, methacrylic acid, ethacrylic acid, and methacrylate esters, such as the methyl, ethyl, butyl, benzyl, phenylethyl, phenoxyethyl, epoxypropyl, and hydroxypropyl methacrylate esters, maleic anhydride, and N-phenyl maleimide. Free-radical-polymerizable dienes, such as butadiene, isoprene and their derivatives, also can be used. Multiple monomers from the same or different classes may be employed.
Of the various vinyl monomers that can be used, styrene, acrylonitrile, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate and mixtures thereo~ are preferred. Two or more monomers may be grafted simul-taneously onto the olefin polymer material by the present process to produce different homopolymer or copolymer grafts or both on the olefin polymer backbone depending or-the relative reactivity of the monomers employed.
Alpha-methylstyrene and maleic anhydride will graft, but do not readily homopolymerize. Hence they must be used in combination with another vinyl compound, such as styrene, with which they copolymerize and which is capable of ~ree radical-initiated polymerization.
The grafting monomer, if liquid at room temperature, can be used neat or in combination with a solvent or diluent which is inert with respect to the particulate polymer material and is not polymerizable by free radicals. If a solid at room temperature, the grafting monomer can be used in solution in a solvent therefore which is inert as set forth above. Mixtures of neat monomer, diluted monomer, and/or dissolved monomer can be used. In all cases, whether or not a solvent or diluent ;s present, the amount of grafting monomer given above (i.e., about from 5 to 240 parts by weight per 100 parts by we~qh~
of olefin polymer material) is based on the actual monomer content.
When a diluent for the monomer is used, less than about 70%, preferably no more than about 50%, and most preferably no more than about 25% by weight, based on the weight of the monomer and the diluent, is used to avoid excessive drops in graft level. Use of solvent in excess of the amount required to dissolve the monomer should be avoided for the same reason.
Solvents or diluents useful in the practice of the method of this invention are those compounds which are inert as described above and which have a chain-transfer constant of less than about 1 x 10 3. Suitable solvents or diluents include ketones, such as acetone; alcohols, such as methanol; aromatic hydrocarbons, such as benzene and xylene; and cycloaliphatic hydrocarbons, such as cyclohexane.
In the method of the invention the particulate olef in polymer material is maintained in a substantially non-o~idizing atmosphere, e.g., under inert gas, during such time that free radicals are present therein. The olefin polymer material is also maintained in such an atmosphere during the formation of the free radicals. The reason for this is that, upon exposure to an oxidizing atmosphere such as air, the free radicals are converted ~o peroxy radicals, which visbreak or degrade the polymer material thereby causing substantial reductions in molecular weight with concomitant increases in melt flow rate. Moreover, with essentially all monomers, the presence of large amounts of air during the treatment with monomer interferes with the graft polymerization ~L ~e.
Therefore, the treatment of the polymer with the initiatof and with the grafting monomer is carried out in a substantially non-oxidizing atmosphere, as are the subsequent steps of the method.
203:~671 The expression "substantially non-oxidizing", when used herein to describe the environment or atmosphere to which the olefin polymer material is exposed, means an environment in which the active-oxygen concentration, i.e., the concentration of oxygen in a form that will react with the free radicals in the polymer material, is less than about 15%, preferably less than about 5%, and most preferably less than about 1%, by volume. The most preferred concentration of active oxygen is 0.004% or lower by volume. Within these limits, the non-oxidizing atmosphere can be any gas, or mixture of gases, which is oxidati~ely inert toward the free radicals in the olein polymer material, e.g., nitrogen, argon, helium, and carbon dioxide.
After the olefin polymer material has been maintaine~
in contact with the monomer for the selected period of time, the resulting graft copolymer, while still maintained in a substantially non-oxidizing environment, is treated, preferably by heating, so as to decompose any unreacted initiator, if any, and to deactivate substantially all o~
the residual free radicals therein. This substantially completely eliminates the possibility of the formation ~f peroxy radicals in the graft copolymer upon its exposure to air, which radicals can cause visbreaking or degradation o~
the polymer. Generally, heating at a temperature of at least about 110C for at least about 5 minutes, preferably at least 120C for at least 20 minutes, is sufficient.
Any unreacted grafting monomer is removed from the graft copolymer, either before or after any unreacted initiator has been decomposed and any residual free radicals have been deactivated, or at the same time as the latter step. If the removal is efected before or during the final decomposition and/or deactivation, a substantially non-o~idizing environment is maintained.
Preferably, any unreacted grafting monomer is removed a~tef any unreacted initiator has been decomposed and any residual ~ree radicals have been deactivated, or during the decomposition/deactivation. In one preferred embodiment, the monomer is removed from the graft copolymer in a nitrogen (or other inert gas) purge at the selected initiator-decomposition temperature, e.g., about 120C.
The following examples, presented for illustrative purposes, describe various embodiments of the method of the invention. Unless otherwise indicated, all parts and percentages are by weight, and all initiator amounts are on an active basis. All melt flow rates (MFRs) for the gra~t copolymers produced were measured on the e~truded and pelletized copolymer.
~ample 1 15 Four hundred grams of a finely divided porous propylene homopolymer (LBD-406A commercially available fro~
HIMONT Italia S.r.l.) are placed in a 2-liter glass reactor equipped with a heating jacket and a helical impeller. Th~
polymer is in the form of generally spherical particles having the following characteristics: nominal melt f low rate (ASTM Method D 123~-82, Condition L) 8 dg/min; intrin-sic viscosity (method of J. H. Elliott et al., J. Applied Polymer Sci. 1~, 2947-2963 (1970) - polymer dissolved in decahydronaphthalene at 135C) 2.4 dl/g; surface area (B.E.T.) 0.34 m2/g; weight average diameter 2.0 mm; and pore volume fraction (mercury porosimetry method) 0.33.
More than 90% of the pores in the porous particles are larger than 1 micron in diameter.
The reactor is purged with nitrogen at room temperature for 15 minutes (to an active o~ygen content of less than 0.004% by volume) and then heated to 100C by circulating hot oil through the reactor jacket, and equil brated to that temperature while nitrogen purging and stirring at 225 rpm continued. Thereafter, purging is stopped, the reactor pressure is adjusted to 14 kPa, and 8 ml of an oxygen-free mineral spirit solution of tert-butylperoxy-2-ethylhexanoate containing 4.0g of the peroxy ester is sprayed onto the hot polymer. This peroxy ester has a half-life of 26 minutes at 100C. After 10 minutes, 283 9 of styrene, which had been purged with nitrogen at 5-10C, is sprayed into the reactor at a rate of 1.20 pph (parts per 100 parts polypropylene, by weight) per minute.
The total addition time is 60 minutes. The reactor is maintained at 100C and stirring continued for 60 minutes a~ter all of the styrene had been added, the temperature o~
the sprayed polymer rising approximately 5-10C owing to the reaction exotherm.
At the end of the grafting period, the reactor is purged with nitrogen for 15 minutes, and the reactor contents then are heated to 120C by purging with heated nitrogen. The reactor temperature is maintained at 120C
for 20 minutes during which time any unreacted styrene monomer is swept out of the reactor in the nitrogen flo~.
After cool-down under a nitrogen blanket, the ree-flowin~
solid product remaining in the reactor is discharged therefrom, dried, and weighed. It weighed approximatelr 677 grams. Analysis o this product indicated that 98% of the styrene had been converted to polystyrene. Analysis ~f the insoluble portion of the product which remained afte~
So~hlet e~traction with methyl ethyl ketone at 80C for 2 hours indicated that the polystyrene content o~ the polystyrene-grafted polypropylene is 37.5~, i.e., a graft level of 60.0 pph from a styrene feed level o 70.8 pptl The graft efficiency (graft level/total polystyrene) is 86%. The MFR of the grat copolymer is 1.6 dg/ min.
E~ample 2 The procedure and ingredients of Example 1 are used with the exception that the amount of propylene homopo~y~r 20~3671 used is 350g, the amount of the peroxy compound used is 79, the amount of styrene used is 2489, the styrene feed rate is 1.22 pph/min, and the delay between peroxide and styrene additions is 20 minutes. The conversion is 98%, the gra~t level 56.1 pph, the graft efficiency 81%, and the MFR 0.2 dg/min.
Example 3 The procedure and ingredients of Example 1 are used with the exception that the styrene and the peroxy ester are mixed together at 5-10C in a capped glass bottle, and, a~ter purging with nitrogen for approximately 15 minutes, the resulting homogeneous solution is sprayed over the hot polymer at a rate of 1.28 pph/min (addition time: 55 minutes). The conversion is 100%, the graft level 58.8 pph, and the graft efficiency 83~. The MFR is 2.1 dg/min.
E~ample 4 The procedure and ingredients of Example 3 are used e~cept that the amount of propylene homopolymer used is 350 g, the amount of the pero~y compound used is 3.59, ~he amount of styrene used is 248 g, and the styrene/initia~r feed rate is 0.35 pph/min (addition time: 3.4 hours). T~e conversion is 98%, the graft level 61.8 pph, the graft efficiency 88%, and the MFR 2.1 dg~min., F~amples 5 - 11 The procedure and ingredients of Example 1 or 3 are used with variations in styrene feed level and/or feed ra~
as set forth in Table I. The results are also shown in Table I.
TABLE I
Styrene Feed Rate Conv. Graft Level Graft Eff. MER
E~ No. Proced~reFeed (p~h) pph/min ~ pph ~ (dq/min) EY. 1 70.8 2.36 98 59.3 86 0.8 6 Es. 3 70.8 2.42 98 57.8 83 2.2 7(a) EY. 1 101.1 1.37 96 85.0 87 0.8 8(a) EY. 3 101.1 1.37 100 95.3 94 1.0 g(b) EY. 1 40.4 1.01 97 35.8 91 4.4 10(C) EY. 1 30.3 4.04 87 23.1 87 5.0 10 ll(d) EY. 3 20.2 4.04 98 17.8 90 5.6 (a) 350g polypropylene, 3.5g peroYy compound, 354g styrene (b) Reactor temperature: 80C; peroYide half-life: 230 min; delay between pero~ide and styrene additions: 15 min. 450g polypropylene, 4.5g peroxy compound, 182g styrene (c) Reactor temperature: 120C; peroxide half-life: 4 min; delay between peroxide and styrene 15 additions: 5 min. 450g polypropylene, 4.5g peroxy compound, 136g styrene (d) 450g polypropylene, 4.5g peroYy compound, 91g styrene.
o C~
Control ~xperiments 1 - 3 The procedure and ingredients of Example 1 are used for Control Experiment 1 with the exception that 3509 of the propylene homopolymer, 3.59 of the peroxy compound, and 248g of the styrene are used, and the styrene is sprayed into the reactor at a rate of 4.5 pph/min (total addition time: 16 minutes). The conversion is 95%, and the gra~t efficiency 62~. The MFR is 3.1 dg/min.
The procedure and ingredients of Example 3 are used for Control E~periment 2 with the exception that 350g of the propylene homopolymer, 3.5g of the peroxy compound, and 248g of the styrene are used, and the styrene is sprayed into the reactor at a rate of 4.5 pph/min (total addition time: 16 minutes). The conversion is 96%, and the graft efficiency 40%. The MFR is 2.9 dg/min.
The procedure and ingredients of Example 9 are used for Control Experiment 3 except that the reactor temper-ature is 130C, the peroxide half-life is 1 min at 130C, and the styrene feed rate is 0.95 pph/min. The graft e~ficiency is 91%, but the conversion is only 44%. The MFQ
is 6.5 dg/min.
Examples 12 - 13 The procedure and ingredients of Example 9 are used except that 4.5 9 of tert-butyl peroxypivalate (E~ample l2) and a mixture of 2.25 g of tert-butylperoxy 2-ethylhexa-noate and 2.2S g of 1,1-dimethyl-3-hydroxybutylperoxy 2-ethylhe~anoate (Example 13) are substituted for the pero~y ester used in E~ample 9.
In Example 12, the initiator half-life is 32 minutes and the styrene feed rate 0.95 pph/min. The conversion i5 93~, the graft level 33.6 pph, the gra~t efficiency 89%
and the MFR 3.4 dg/min.
In E~ample 13, the reactor temperature is 90C, the initiator half-lives are 80 minutes and 20 minutes, respectively, the styrene feed rate is 1.01 pph/min, and the delay between peroxide and styrene additions is 10 minutes. The conversion is 98%, the graft level 35.1 pph, the graft efficiency 88%, and the MFR 7.5 dg~min.
S EYamDle lq The procedure and ingredients of Example 3 are used e~cept that the styrene feed level (1629 added) is 90.4 pph, the styrene addition rate is 1.14 pph/min, and the polypropylene used is Pro-fax 6501 having an IV of 2.5 dl/g, a MFR of 4.0 dg/min, a surface area (8.E.T) of 2.n m2/g, a pore volume fraction (by mercury porosimetry) o~
0.15, a weight average diameter of 0.2 mm, a bulk density of 0.53 g/ml, and a solubility in methylene chloride of 1.~
wt %. None of the pores in the particles are larger than 1 micron in diameter. The conversion is 93%, the graft level 31.0 pph, and the graft efficiency ~2%.
E~amPle 15 The procedure and ingredients of E~ample 3 are used e~cept that methyl methacrylate (29 pph) is used instead of styrene, the monomer/initiator mixture is added at a rate of 1.01 pph~min and the reactor temperature is ~5C. The amount of propylene homopolymer used is 4509, peroxy com-pound 4.5g, and methyl methecrylate 1359. The conversion is 86~, graft level 23.5 pph, and graft ef~iciency 90~.
ExamPle 16 The procedure and ingredients of E~ample 1 are used e~cept that methyl methacrylate (31.3 pph) is substituted for styrene, di(4-tert-butylcyclohe~yl)pero~y dicarbona~e (0.49 pph) is substituted for the pero~y ester, the amount of propylene homopolymer used is 4509, the reactor temper-ature is 70C, and the monomer is added at a rate of l.q pph/min. The conversion is 98%, the graft level 26.7 pph, the graft efficiency 85%, and the MFR 3.2 d~/min.
Example 17 The procedure and ingredients of Example 1 are used except that butyl acrylate (17.6 pph) is used instead of styrene and added at a rate of 1.17 pph/min (over 15 minutes), and 0.63 pph of the peroxy compound and a larger reactor are employed. The reactor is maintained at 105C
for 3 hours after all of the monomer had been added. A
vacuum then is applied at 104C for 1 hour followed by a 4-hour nitrogen purge at 120C. The conversion level is approximately 16.0 pph, the conversion 91%, and the MFR
10.4 dg/min.
~ample 18 The procedure and ingredients of Example 17 are used except that an ethylene/propylene random copolymer having an ethylene content of about 4.0% is substituted for the propylene homopolymer, and a mixture of styrene (4.42 pph and butyl acrylate (13.24 pph~ is used instead of butyl acrylate and added at a rate of 1.18 pph/min. (over 15 minutes). The pero~ide addition level is 0.5 pph, and the reactor temperature 100C. The four-hour nitrogen purge i5 at 100C. The conversion level for both monomers is 17.6 pph, the conversion 100%, and the MFR 9.7 dg/min.
~Yample 19 The procedure and ingredients of Example 17 are used e2cept that a chemically blended EPR-modified propylene homopolymer having a MFR of 4.89 dg/min, a polypropylene content of about 88%, and an EPR content of about 12%, wit~
an ethylene content of about 8%, is substituted for the propylene homopolymer, and styrene (53.8 pph) is substituted for the butyl acrylate. The styrene addit~on rate is 1.79 pph/min (30-minute addition period). The reactor temperature is 101C, and the peroxide addition level 0.2S pph. The nitrogen purge is conducted at 100C
for 5 hours. The conversion level is 45.5 pph, the conversion 85%, and the MFR 2.2 dg/min.
Example 20 The procedure and ingredients of Example 19 are used except that the EPR-modified propylene homopolymer used had a polypropylene content of 40~ and an EPR content of 60%, with an ethylene content of 39%, and a MFR of 16 dg/min.
The conversion level is 53.8 pph, the conversion 100~, and the MFR 2.1 dg/min.
Control ~periment 9 The procedure and ingredients of Example 17 are used with the following exceptions:
Pro-fax 6301 polypropylene having a MFR of 12.0 dg/min, a pore volume fraction of 0.15, and a weight average diameter of 0.2 mm is used instead o~ LBD-460A.
None of the pores in the particles are larger than 1 micron in diameter. The grafting monomer is n-butyl methacryla~e (17.1 pph), added at a rate of 0.56 pph/min (over a peri~d of 23 minutes). The initiator is tert-butyl-2-ethylhexyl-pero~y dicarbonate (1.3 pph), the reactor temperature is 135C., and the product is vacuum-dried at 135C for 5 hours. The conversion is 77%, and the MFR 152 dg/min.
E~ample 21 The procedure and ingredients of Example 1 are use~
e~cept that 1952g of propylene homopolymer is used instea~
of 400g, a 10 liter steel reactor is used instead of a 2 liter glass reactor, and the procedure was changed as se~
forth below.
The reactor is purged with nitrogen at room temperature until the active oxygen level reached 20 ppm and then heated to 120~C (+/- 1.5C) by circulating hot oil through the reactor jacket, and equilibrated to that tem-perature while nitrogen purging and stirring at 190 rpmcontinued. Styrene (12809), acrylonitrile (408.6g) and an oxygen-free mineral spirit solution of tert-butylperoxy 2-ethylhexanoate (78g o~ solution, 50% by weight of mineral s~irits) are added to a steel pressure cylinder and purged with nitrogen. The monomers/pero~ide mixture is fed to the reactor contents at a rate of 1.02 pph (parts per 100 parts polypropylene, by weight) per minute while maintaining the temperature of the reactor contents at 120~C (+/- 1.5C).
The total addition time is 85 minutes. The reactor is maintained at 120C with stirring for an additional 30 minutes following complete addition of the monomers. At the end of the grafting reaction period, a vacuum was drawn on the reactor contents and the temperature increased to 140C. The total heat up time under vacuum was 22.8 minutes. Once the temperature reached ls0C, the vacuum was broken with nitrogen and the contents purged with nitrogen for 30 minutes. After cool-down under a nitrogen blanket, the free-flowing solid product remaining in the reactor is discharged therefrom, dried, and weighed. Final weight of the product is 3597.7 grams, representing a conversion of 97.3%.
Other features, advantages and embodiments of the invention disclosed herein will be readily apparent to those e~ercising ordinary skill after reading the foregoin~
disclosures. In this regard, while specific embodiments ot the invention have been described in considerable detail, variations and modifications of these embodiments can be effected without departing from the spirit and scope o~ th~
invention as described and claimed.
Graft copolymers of polypropylene have been of interest for some time because they are capable of possessing some properties o~ the grated polymer (produced by the homo- or copolymerization of the monomer or monomers, respectively) as well as of the polypropylene backbone. It has been suggested, for e~ample, that some o~
these graft copolymers be used as compatibilizers for normally immiscible polymer systems and as components o~
gum plastic compositions.
The preparation of graft copolymers by creating acti~e sites on the main polymer chain or backbone, and initiatirlq graft polymerization of a polymerizable monomer at these sites, is well-known. Procedures which have been used or introducing such active sites into the polymer chain have included treatment with organic chemical compounds capable of generating free radicals, and irradiation. In the chémical method, àn organic chemical compound capable o~
generating free radicals, such as a peroxide or azo compound, is decomposed in the presence of the backbone polymer with the formation of free radicals, which form ~e active grafting sites on the polymer and initiate the polymeriz~tion of the monomer at these sites.
Of the various techniques which have been employed for preparing gra~t copolymers o~ polyolefins by the chemic~l method of free radical generation, the bulk technique, i~
which the polymer particles are contacted directly with 20:~3671 , initiator and monomer, without the intervention of a liquid suspending medium or a solvent, is advantageous in terms of simplicity of execution and the avoidance of side-reactions caused by the presence of certain solvents or suspending media, such as water. However, regardless of the physical state of the polymer to be grafted, the grafting process is subject to problems such as degradation of the polyolefin, possibly leading to a graft copolymer having an undesirably high melt flow rate, and excessive formation of the homopolymer of the grafting monomer at the expense of the formation of the polyolefin graft copolymer.
U.S. Patent 4,595,726 discloses graft copolymers of 3-100%, preferably 3-30%, by weight of an alkyl meth-acrylate moiety grafted onto a polypropylene backbone. The lS graft copolymers, useful as adhesives in polypropylene laminates, are prepared at a temperature below the softening point of polypropylene by a solvent-free reaction, reportedly vapor-phase, between polypropylene an~
the methacrylate monomer in the presence of a free-radical-forming catalyst. A preferred initiator is tert-butyl perbenzoate, stated as having a 15-minute half-life at 135 C, and reactor temperatures of 135C and 140C are disclosed. Degradation of the polypropylene chain due to the reaction conditions employed is reported. Immediately after the pero~ide is added to the polypropylene, the monomer is added over a time period which is fi~ed by the half-life of the pero~ide initiator (i.e., 1-2 half-lives) In other words, according to the teachings of U.S. Patent 4,595,726, for a given initiator half-life, it is necessd~y to employ a higher rate of addition of the monomer as the total amount of monomer to be added increases.
The preparation of "graft-type copolymers by dissolving an organic pero~ide in a monomer and adding th~
solution to free-flowing particles of the base polymer, particularly polyvinyl chloride, is described in U.S.
Patent 3,240,843. The "graft-type" products are described as having monomeric, as opposed to polymeric, branches attached to the polymer backbone. Homopolymerization of the monomer also is mentioned. To avoid particle agglomeration, the amount of monomer added cannot exceed the maximum absorbable by the polymer particles. In the case of polypropylene charged into a reactor with a solution containing styrene, butadiene, acrylonitrile, and benzoyl pero~ide, the total amount of monomers added is only 9% of the amount of polypropylene charged.
The present invention provides a method of making an olefin polymer graft copolymer wherein free radical sites are produced in a particulate olefin polymer material by treating the polymer material at a temperature of about from 60 to 125C with about from 0.1 to 6.0 pph (parts by weight per 100 parts by weight of the olefin polymer material) of an organic chemical compound which is a free radical polymerization initiator and has a decomposition half-life of about from 1 to 240 minutes at the temperature employed.
Over a time period which coincides with, or follows, the period of initiator treatment, with or without overlap the polymer material is treated with about from S to 240 pph of a grafting monomer which is capable of being polymerized by free radicals, the temperature employed during any period of monomer treatment being as indicated above with respect to initiator treatment. The addition of the grafting monomer to the polymer material is controlled so that at all addition levels of about from 5 to 240 pph the rate of addition does not e~ceed about 4.5, pre~erably does not e~ceed about 4.0, and most preferably does not e~ceed about 3.0, pph per minute.
After the grafting period, i.e., the period o~
treatment with the grafting monomer, and any hold period at reaction conditions subsequent thereto, any unreacted monomer is removed from the resultant grafted particulate olefin polymer material, and the decomposition o~ any unreacted initiator and deactivation of any residual free radicals are promoted, e.g., by a temperature increase.
During the entire process the polymer material is maintained in a substantially non-oxidizing environment.
The method of this invention embodies a combination of steps which together permit olefin polymer graft copolymers to be obtained not only in high conversions (monomer consumption) but also with a high degree of graft efficiency. Moreover, degradation of the backbone olefin polymer is minimized, thereby avoiding the production of a graft copolymer having a melt flow rate which is sub-stantially higher than that of the starting backbone olefin polymer, a condition that can adversely afect the processing behavior of the graft copolymer.
While not wishing to be bound or limited in any way by theoretical considerations, we believe that the high degree of eficiency afforded by the method of the invention is related to the manner in which the grafting monomer is brought into contact with the olefin polymer particles in which free radical sites have been, and/or are being, produced by contact of the initiator with the heated particles. The low rate of addition of the monomer, i.e., a rate not e~ceeding about 4.5, preferably no greater than about 4.0, and most preferably no greater than about 3.0, pph per minute, creates an essentially ~dryn condition in which the monomer liquid and the initiator come together in the presenCe of heat (i.e., that needed to decompose the initiator) instead of in a large volume of monomer liquid.
It has been found that homopolymerization of the monomer, at the e~pense of a graft polymerization reaction, becomes more prevalent at rates of monomer addition which resul~ ~n a buildup of monomer liquid within and between polymer particles. It is believed that, in the latter case, the ;
so-called "wet" condition due to the buildup of ~o~m~
liquid may facilitate or promote the sel-polymerization of the monomer rather than graft polymerization with the olefin polymer particles.
In the present process, the monomer feed rate can be as low as desired, and the minimum generally will be dictated by the capability of available equipment and economic considerations. While rates of at least about 0.1 - 0.2 pph/min can be used, a preferred practical minimum is about 0.3 pph/min. Preferred rates in any particular case will depend on such factors as the monomer feed level, the initiator/monomer addition mode, and the reactivity of the particular monomer used.
The addition of monomer at a rate of about from 0.1 to 4.5 pph/min, preferably about from 0.3 to 4.0 pph/min and most preferably 0.3 to 3.0 pph/min results in high graft efficiencies with high monomer conversions over a wide range of monomer feed levels. The monomer addition rates set forth above, including those above the preferred ma~imum, are suitable with lower monomer feed levels, e.g., levels of up to about 40 pph. Also, a maximum monomer addition rate of about 4.0 pph/min is preferred provided that the monomer feed level does not exceed about 40 pph.
With feed levels above about 40 pph, addition rates of about 0.3 to about 3.0 pph/min are used to provide high graft efficiencies. Such rates are most preferred in the present process because of their applicability over a wider range of monomer feed levels. With the most preferred monomer addition rates, and especially at rates up to abo~t 3.0 pph~min, high graft efficiencies are attained at hi~h monomer conversions regardless of addition mode even at high monomer feed levels of 100 pph and above.
The above-specified monomer addition rate must be adhered to at all addition levels of monomer to be adde~, i.e., addition levels of about from 5 to 240 pph, and is ~f 20:~3571 increasingly qreater importance at higher addition levels.
In contrast, the fixed addition time advocated by the aforementioned U.S. Patent 4,595,726 results in the use of the highest monomer addition rates at the highest addition levels, i.e., the very levels at which, according to the present invention, low addition rates are most important.
A fixed addition time, e.g., 1-2 half-lives of an initiator such as tert-butyl perbenzoate, as taught in the afore-mentioned patent, will not be long enough to result in a sufficiently low addition rate at the large monomer additions needed to produce high graft levels with a hiyh degree of efficiency.
In one embodiment of the present method, the time period during which the mass of olefin polymer particles is treated with the grafting monomer follows the time period during which the particle mass is treated with the initiator. In this case (separate-addition mode), the initiator is added first to the particles, which are preferably heated to the temperature being used, and the production of free radical sites in the olefin polymer material begins. The addition of the monomer may begin immediately after the addition of the initiator has been completed, or after a delay or hold time subsequent to the completion of the initiator addition. Separate additions also can be multi-staged whereby the additions are incre-mental and the initiator/monomer addition sequence is repetitive. In another embodiment, the initiator and the monomer are added to the heated polymer particles at the same time (côncurrent-addition mode), e.g., by combininq the initiator (neat or a liquid solution thereof) and the monomer (neat or a liquid solution thereof~ at a temper-ature at which no appreciable decomposition of the initiator occurs. The concurrent addition of separate initiator and monomer streams also can be employed, as ~ell as a combination of separate addition and concurrent 20336~1 ._ addition, in which the monomer addition period follows the initiator addition period with overlap. Whether the initiator and monomer are added concurrently or monomer addition follows initiator addition, either the initiator S or monomer, or both, can be added continuously or intermittently. The method of the invention can be carried out as a semi-batch, semi-continuous, or continuous process.
In the present process the particulate olefin polymer material which is treated with the initiator and the grafting monomer is at a temperature of about from 60 to 125C, preferably about from 80 to 120C. While temperatures below about 60C can be used, the decomposi-tion half-life of many free radical initiators at such temperatures is so long as to be impractical, and initiators having a short enough half-life below about 60C
often are difficult to handle. Above about 125C, the sharp reduction in decomposition half-life which occurs with many initiators causes the monomer conversion to dro~, especially in the separate-addition mode. Moreover, initiators having longer half-lives at temperatures abo~e about 125C tend to have an adverse effect on the ole~in polymer and/or the resulting graft copolymer.
Treating the olefin polymer material with the initiator and the monomer at a temperature as set forth above provides an initiator half-life of about from 1 to 240 minutes. After the addition of the monomer, the thus-treated polymer material may be maintained at the selected temperature for at least about 3, and most preferably at least about 10, minutes. This hold period may be e~tended to several hours, especially at lower temperatures. Preferably the initiator and temperature will be selected to allow grafting to be completed within about 2 to 10 initiator half-lives. Conditions that ~e~ul~
in half-lives below about 2 minutes are not preferred, especially in the separate-addition mode with delayed 2~33671 .
monomer addition, inasmuch as the conversion may be deleteriously affected if the initiator is allowed to decompose rapidly before the monomer addition begins.
To assure a high conversion and graft efficiency, and effective use of the initiator, a time of at least about 1, preferably at least about 2, initiator half-lives at the selected temperature should elapse between the start of the initiator addition period and the end of the monomer removal step. The time from the start of monomer addition to the end of the grafting period depends on the amount of monomer used and the rate of addition, longer times being used at lower temperatures and higher monomer feed levels.
At the monomer addition rates used in the present process, the hold period, if any, after completion of the monomer addition generally is as stated above, longer hold periods after monomer addition preferably being used at lower temperatures and higher monomer feed levels. In the separate-addition mode, preferably no more than about 2.5 initiator half-lives should separate the initiator and monomer addition periods to assure the availability of ttle necessary free radicals once the addition of the monomer begins.
The olefin polymer material useful in the practice o~
the method of this invention for making graft copolymers of olefin polymers is (a) a homopolymer of a linear or branched C l-olefin; (b) a random copolymer of a linear or branched C2 8 l-olefin with a different olefin selected from the group consisting of C2 10 l-olefins, provided that, when the different olefin is ethylene, the ma~imum polymerized ethylene content is about 10~, prefer-ably about 4%, by weight; when the olefin is propylene and the different olefin is a C4 10 l-olefin, the maximum polymerized content thereof is about 20~, preferably abo~t 16%, by weight; and when the olefin is ethylene and the different olefin is a C3 10 l-ole~in, the maximum poly-merized content thereof is about 10%, preferably about 5%,by weiQht; (c) a random terpolymer of a linear or branched C3 8 l-olefin and two different olefins selected from the group consisting of ethylene and C4 8 l-olefins, provided that the maximum polymerized content o~ the different C4 8 l-olefins is about 20%, preferably about 16%, by weight, and, when ethylene is one of the different olefins, the ma~imum polymerized ethylene content is about 5%, preferably about 4%, by weight; or (d) a homopolymer of (a) or a random copolymer of (b) which is impact-modified with about from 10 to 60% of (i) an ethylene-propylene rubber having an ethylene content of about from 7 to 70%, preferably about from 7 to 40~, most preferably about from 10 to 40%, (ii) an ethylene/butene-l copolymer rubber (E~
having an ethylene content of from 30 to 70%, (iii) a propylene/butene-l copolymer rubber (PBR) having a butene-l content of from 30 to 70%, (iv) an ethylene-propylene-non-conjugated diene monomer rubber (EPDM) having an ethylene content of 30 to 70% and diene content of from 1 to 10%, (v) an ethylene/propylene/butene terpolymer rubber (~PBR) having a propylene content of from 1 to 10% and butene content of from 30 to 70% or a propylene content of from 30 to 70% and butene content of from 1 to 10%.
The C2 8 l-olefins which can be used in the preparation of the olefin polymer materials as described above include, for example, ethylene, propylene, l-butene, isobutylene, 3-methyl-1-butene, 3,4-dimethyl-1-butene, l-pentene, 4-methyl-1-pentene, l-hexene, 3-methyl-1-hexene l-heptene and the like. Propylene and l-butene are the preferred C3-C8 l-olefin monomers.
C3 10 l-olefins which can be used in the preparation of the olefin polymer materials as described above include linear and branched olefins such as those listed above ~or the C2 8 l-olefins which have at least 3 carbon atoms.
When the olefin polymer is an ethylene homopolymer, it has a density of 0.91 g/cm3 or greater, and when the olefin polymer is an ethylene copolymer with a C3 10 alpha-olefin, it has a density of 0.91 g/cm3 or greater.
Suitable ethylene copolymers include ethylene/butene-l, ethylene/hexene-l and ethylene/4-methyl-1-pentene. The ethylene copolymer can be a HDPE or a LLDPE, and the ethylene homopolymer can be a HDPE or a LDPE. Typically the LLDPE and LDPE have densities of 0.91 g/cm3 or greater and the HDPE have densities of 0.95 g/cm3 or greater.
The impact-modified olefin polymer can be prepared by first polymerizing a C2 8 l-olefin to form a homopolymer of said olefin, or copolymerizing such an olefin with a different olefin selected from C2 10 l-olefins, and then polymerizing the relevant monomers to form the rubber in the presence of said homopolymer or copolymer in a reactor or series of reactors. Alternatively, mechanical blends can be prepared by separately polymerizing 1) the parti-cular olefin to form the homo- or copolymer and 2) the relevant monomers to form the rubber, and then physically mixing the homo- or copolymer with the rubber until a homogeneous blend is obtained. Reactor blends are preferred when an impact-modified olefin polymer is used.
Homopolymers of butene-l, HDPE and LLDPE are preferred. Homopolymers, random copolymers, random terpolymers, and impact-modified homopolymers and copolymers of propylene are also preferred and are the most preferred olefin polymer materials for use in the present process and are referred to herein, individually or collectively, as propylene polymer materials.
Suitable particulate forms of the olefin polymer material used in the present method include powder, 1ak~, granulate, spherical, cubic and the like. Spherical particulate forms are preerred. The pore volume raction _ of the particles can be as low as about 0.04, but it is preferred that the grafting be effected on olefin polymer particles having a pore volume fraction o~ at least 0.07.
Most preferably, the olefin polymer used in the present method will have a pore volume fraction of at least about 0.12, and most preferably at least about 0.20, with more than 40%, preferably more than 50%, and most preferably more than 90%, of the pores having a diameter larger than 1 micron, a surface area of at least 0.1 m /g, and a weight averagè diameter of about from 0.4 to 7 mm. In the preferred polymer, grafting takes place in the interior o~
the particulate material as well as on the external surfaoe thereof, resulting in a substantially uniform distribution of the graft polymer throughout the ole~in polymer particle.
According to the method of the invention, free radical or active sites are produced in the particulate olefin polymer material by treating the polymer material with an organic compound which is a free-radical-generating polymerization initiator and has a decomposition half~
at the temperature employed o~ about from 1 to 240, preferably about from 5 to 100, and most preferably about from 10 to 40, minutes. Organic peroxides, and especially those which generate alkoxy radicals, constitute the preferred class of initiators. These include acyl peroxides, such as benzoyl and dibenzoyl pero~ides; dialkyl and aralkyl pero~ides, such as di-tert-butyl peroxide, dicumyl peroside, cumyl butyl pero~ide, l,l-di-tert-butylpero~y-3,5,5-trimethylcyclohexane, 2,5-dimethyl-2,5-di-tert-butylpero~yhexane, and bis(alpha-tert-butyl pero~yisopropylbenzene); pero~y esters, such as tert-butyl-pero~ypivalate, tert-butyl perbenzoate, 2,5-dimethylhexyl 2,5-di(perbenzoate), tert-butyl di(perphthalate), tert-butylpero~y-2-ethyl he~anoate; and 1,1-dimethyl-3-hydro~y-butylpero~y-2-ethyl hexanoate; and pero~y carbonates, such as di(2-ethylhe~yl) pero~y dicarbonate, di(n-propyl)per~y dicarbonate, and di(4-tert-butylcyclohexyl)peroxy dicar-bonate. Azo compounds, such as azobisisobutyronitrile, also may be used. Two or more initiators having the same or di~ferent half-lives may be employed.
The initiator, if a liquid at the decomposition temperature used, may be used neat or in solution. I~ a solid at the decomposition temperature used, it may be dissolved in a suitable liquid solvent. The concentration of the initiator in solution typically should be about ~rom 5% to g8% by weight. Peroxide initiators are available in hydrocarbon solutions at a concentration of about ~rom 12.5 to 75 weight %. Whether neat or in solution, the activ~
concentration of the initiator Der se should be about ~rom 0.1 to 6.0 pph, preferably about from 0.2 to 3.0 pph, to assure the generation of a sufficient number of free radical sites on and in the olefin polymer material.
The grafting monomers useful in accordance with this invention may be any monomeric vinyl compound capable o~
being polymerized by ~ree radicals wherein the vinyl radical, H2C~CR-, in which R , H or methyl, is attached to a straight or branched aliphatic chain or to a substituted or unsubstituted aromatic, heterocyclic, or alicyclic ring in a mono- or polycyclic compound. Typical substituent groups may be alkyl, hydro~yalkyl, aryl, and halo. Usually the vinyl monomer will be a member of one of the following classes: (1) vinyl-substituted aromatic, heterocyclic, or alicyclic compounds, including styrene, vinylnaphthalene, vinylpyridine, vinylpyrrolidone, vinylcarbazole, and homologs thereof, e.g., alpha- and para-methylstyrene, methylchlorostyrene, p-tert-butyl-styrene, methylvinylpyridine, and ethylvinylpyridine; (2) vinyl esters of aromatic and saturated aliphatic carboxYItC
acids, including vinyl formate, vinyl acetate, vinyl chloracetate, vinyl cyanoacetate, vinyl propionate, and vinyl benzoate; and (3) unsaturated aliphatic nitri les an4 carboxylic acids and their derivatives, including acry-lonitrile, methacrylonitrile, acrylamide, methacrylamide, acrylic acid, acrylate esters, such as the methyl, ethyl, hydroxyethyl, 2-ethylhexyl, and butyl acrylate esters, methacrylic acid, ethacrylic acid, and methacrylate esters, such as the methyl, ethyl, butyl, benzyl, phenylethyl, phenoxyethyl, epoxypropyl, and hydroxypropyl methacrylate esters, maleic anhydride, and N-phenyl maleimide. Free-radical-polymerizable dienes, such as butadiene, isoprene and their derivatives, also can be used. Multiple monomers from the same or different classes may be employed.
Of the various vinyl monomers that can be used, styrene, acrylonitrile, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate and mixtures thereo~ are preferred. Two or more monomers may be grafted simul-taneously onto the olefin polymer material by the present process to produce different homopolymer or copolymer grafts or both on the olefin polymer backbone depending or-the relative reactivity of the monomers employed.
Alpha-methylstyrene and maleic anhydride will graft, but do not readily homopolymerize. Hence they must be used in combination with another vinyl compound, such as styrene, with which they copolymerize and which is capable of ~ree radical-initiated polymerization.
The grafting monomer, if liquid at room temperature, can be used neat or in combination with a solvent or diluent which is inert with respect to the particulate polymer material and is not polymerizable by free radicals. If a solid at room temperature, the grafting monomer can be used in solution in a solvent therefore which is inert as set forth above. Mixtures of neat monomer, diluted monomer, and/or dissolved monomer can be used. In all cases, whether or not a solvent or diluent ;s present, the amount of grafting monomer given above (i.e., about from 5 to 240 parts by weight per 100 parts by we~qh~
of olefin polymer material) is based on the actual monomer content.
When a diluent for the monomer is used, less than about 70%, preferably no more than about 50%, and most preferably no more than about 25% by weight, based on the weight of the monomer and the diluent, is used to avoid excessive drops in graft level. Use of solvent in excess of the amount required to dissolve the monomer should be avoided for the same reason.
Solvents or diluents useful in the practice of the method of this invention are those compounds which are inert as described above and which have a chain-transfer constant of less than about 1 x 10 3. Suitable solvents or diluents include ketones, such as acetone; alcohols, such as methanol; aromatic hydrocarbons, such as benzene and xylene; and cycloaliphatic hydrocarbons, such as cyclohexane.
In the method of the invention the particulate olef in polymer material is maintained in a substantially non-o~idizing atmosphere, e.g., under inert gas, during such time that free radicals are present therein. The olefin polymer material is also maintained in such an atmosphere during the formation of the free radicals. The reason for this is that, upon exposure to an oxidizing atmosphere such as air, the free radicals are converted ~o peroxy radicals, which visbreak or degrade the polymer material thereby causing substantial reductions in molecular weight with concomitant increases in melt flow rate. Moreover, with essentially all monomers, the presence of large amounts of air during the treatment with monomer interferes with the graft polymerization ~L ~e.
Therefore, the treatment of the polymer with the initiatof and with the grafting monomer is carried out in a substantially non-oxidizing atmosphere, as are the subsequent steps of the method.
203:~671 The expression "substantially non-oxidizing", when used herein to describe the environment or atmosphere to which the olefin polymer material is exposed, means an environment in which the active-oxygen concentration, i.e., the concentration of oxygen in a form that will react with the free radicals in the polymer material, is less than about 15%, preferably less than about 5%, and most preferably less than about 1%, by volume. The most preferred concentration of active oxygen is 0.004% or lower by volume. Within these limits, the non-oxidizing atmosphere can be any gas, or mixture of gases, which is oxidati~ely inert toward the free radicals in the olein polymer material, e.g., nitrogen, argon, helium, and carbon dioxide.
After the olefin polymer material has been maintaine~
in contact with the monomer for the selected period of time, the resulting graft copolymer, while still maintained in a substantially non-oxidizing environment, is treated, preferably by heating, so as to decompose any unreacted initiator, if any, and to deactivate substantially all o~
the residual free radicals therein. This substantially completely eliminates the possibility of the formation ~f peroxy radicals in the graft copolymer upon its exposure to air, which radicals can cause visbreaking or degradation o~
the polymer. Generally, heating at a temperature of at least about 110C for at least about 5 minutes, preferably at least 120C for at least 20 minutes, is sufficient.
Any unreacted grafting monomer is removed from the graft copolymer, either before or after any unreacted initiator has been decomposed and any residual free radicals have been deactivated, or at the same time as the latter step. If the removal is efected before or during the final decomposition and/or deactivation, a substantially non-o~idizing environment is maintained.
Preferably, any unreacted grafting monomer is removed a~tef any unreacted initiator has been decomposed and any residual ~ree radicals have been deactivated, or during the decomposition/deactivation. In one preferred embodiment, the monomer is removed from the graft copolymer in a nitrogen (or other inert gas) purge at the selected initiator-decomposition temperature, e.g., about 120C.
The following examples, presented for illustrative purposes, describe various embodiments of the method of the invention. Unless otherwise indicated, all parts and percentages are by weight, and all initiator amounts are on an active basis. All melt flow rates (MFRs) for the gra~t copolymers produced were measured on the e~truded and pelletized copolymer.
~ample 1 15 Four hundred grams of a finely divided porous propylene homopolymer (LBD-406A commercially available fro~
HIMONT Italia S.r.l.) are placed in a 2-liter glass reactor equipped with a heating jacket and a helical impeller. Th~
polymer is in the form of generally spherical particles having the following characteristics: nominal melt f low rate (ASTM Method D 123~-82, Condition L) 8 dg/min; intrin-sic viscosity (method of J. H. Elliott et al., J. Applied Polymer Sci. 1~, 2947-2963 (1970) - polymer dissolved in decahydronaphthalene at 135C) 2.4 dl/g; surface area (B.E.T.) 0.34 m2/g; weight average diameter 2.0 mm; and pore volume fraction (mercury porosimetry method) 0.33.
More than 90% of the pores in the porous particles are larger than 1 micron in diameter.
The reactor is purged with nitrogen at room temperature for 15 minutes (to an active o~ygen content of less than 0.004% by volume) and then heated to 100C by circulating hot oil through the reactor jacket, and equil brated to that temperature while nitrogen purging and stirring at 225 rpm continued. Thereafter, purging is stopped, the reactor pressure is adjusted to 14 kPa, and 8 ml of an oxygen-free mineral spirit solution of tert-butylperoxy-2-ethylhexanoate containing 4.0g of the peroxy ester is sprayed onto the hot polymer. This peroxy ester has a half-life of 26 minutes at 100C. After 10 minutes, 283 9 of styrene, which had been purged with nitrogen at 5-10C, is sprayed into the reactor at a rate of 1.20 pph (parts per 100 parts polypropylene, by weight) per minute.
The total addition time is 60 minutes. The reactor is maintained at 100C and stirring continued for 60 minutes a~ter all of the styrene had been added, the temperature o~
the sprayed polymer rising approximately 5-10C owing to the reaction exotherm.
At the end of the grafting period, the reactor is purged with nitrogen for 15 minutes, and the reactor contents then are heated to 120C by purging with heated nitrogen. The reactor temperature is maintained at 120C
for 20 minutes during which time any unreacted styrene monomer is swept out of the reactor in the nitrogen flo~.
After cool-down under a nitrogen blanket, the ree-flowin~
solid product remaining in the reactor is discharged therefrom, dried, and weighed. It weighed approximatelr 677 grams. Analysis o this product indicated that 98% of the styrene had been converted to polystyrene. Analysis ~f the insoluble portion of the product which remained afte~
So~hlet e~traction with methyl ethyl ketone at 80C for 2 hours indicated that the polystyrene content o~ the polystyrene-grafted polypropylene is 37.5~, i.e., a graft level of 60.0 pph from a styrene feed level o 70.8 pptl The graft efficiency (graft level/total polystyrene) is 86%. The MFR of the grat copolymer is 1.6 dg/ min.
E~ample 2 The procedure and ingredients of Example 1 are used with the exception that the amount of propylene homopo~y~r 20~3671 used is 350g, the amount of the peroxy compound used is 79, the amount of styrene used is 2489, the styrene feed rate is 1.22 pph/min, and the delay between peroxide and styrene additions is 20 minutes. The conversion is 98%, the gra~t level 56.1 pph, the graft efficiency 81%, and the MFR 0.2 dg/min.
Example 3 The procedure and ingredients of Example 1 are used with the exception that the styrene and the peroxy ester are mixed together at 5-10C in a capped glass bottle, and, a~ter purging with nitrogen for approximately 15 minutes, the resulting homogeneous solution is sprayed over the hot polymer at a rate of 1.28 pph/min (addition time: 55 minutes). The conversion is 100%, the graft level 58.8 pph, and the graft efficiency 83~. The MFR is 2.1 dg/min.
E~ample 4 The procedure and ingredients of Example 3 are used e~cept that the amount of propylene homopolymer used is 350 g, the amount of the pero~y compound used is 3.59, ~he amount of styrene used is 248 g, and the styrene/initia~r feed rate is 0.35 pph/min (addition time: 3.4 hours). T~e conversion is 98%, the graft level 61.8 pph, the graft efficiency 88%, and the MFR 2.1 dg~min., F~amples 5 - 11 The procedure and ingredients of Example 1 or 3 are used with variations in styrene feed level and/or feed ra~
as set forth in Table I. The results are also shown in Table I.
TABLE I
Styrene Feed Rate Conv. Graft Level Graft Eff. MER
E~ No. Proced~reFeed (p~h) pph/min ~ pph ~ (dq/min) EY. 1 70.8 2.36 98 59.3 86 0.8 6 Es. 3 70.8 2.42 98 57.8 83 2.2 7(a) EY. 1 101.1 1.37 96 85.0 87 0.8 8(a) EY. 3 101.1 1.37 100 95.3 94 1.0 g(b) EY. 1 40.4 1.01 97 35.8 91 4.4 10(C) EY. 1 30.3 4.04 87 23.1 87 5.0 10 ll(d) EY. 3 20.2 4.04 98 17.8 90 5.6 (a) 350g polypropylene, 3.5g peroYy compound, 354g styrene (b) Reactor temperature: 80C; peroYide half-life: 230 min; delay between pero~ide and styrene additions: 15 min. 450g polypropylene, 4.5g peroxy compound, 182g styrene (c) Reactor temperature: 120C; peroxide half-life: 4 min; delay between peroxide and styrene 15 additions: 5 min. 450g polypropylene, 4.5g peroxy compound, 136g styrene (d) 450g polypropylene, 4.5g peroYy compound, 91g styrene.
o C~
Control ~xperiments 1 - 3 The procedure and ingredients of Example 1 are used for Control Experiment 1 with the exception that 3509 of the propylene homopolymer, 3.59 of the peroxy compound, and 248g of the styrene are used, and the styrene is sprayed into the reactor at a rate of 4.5 pph/min (total addition time: 16 minutes). The conversion is 95%, and the gra~t efficiency 62~. The MFR is 3.1 dg/min.
The procedure and ingredients of Example 3 are used for Control E~periment 2 with the exception that 350g of the propylene homopolymer, 3.5g of the peroxy compound, and 248g of the styrene are used, and the styrene is sprayed into the reactor at a rate of 4.5 pph/min (total addition time: 16 minutes). The conversion is 96%, and the graft efficiency 40%. The MFR is 2.9 dg/min.
The procedure and ingredients of Example 9 are used for Control Experiment 3 except that the reactor temper-ature is 130C, the peroxide half-life is 1 min at 130C, and the styrene feed rate is 0.95 pph/min. The graft e~ficiency is 91%, but the conversion is only 44%. The MFQ
is 6.5 dg/min.
Examples 12 - 13 The procedure and ingredients of Example 9 are used except that 4.5 9 of tert-butyl peroxypivalate (E~ample l2) and a mixture of 2.25 g of tert-butylperoxy 2-ethylhexa-noate and 2.2S g of 1,1-dimethyl-3-hydroxybutylperoxy 2-ethylhe~anoate (Example 13) are substituted for the pero~y ester used in E~ample 9.
In Example 12, the initiator half-life is 32 minutes and the styrene feed rate 0.95 pph/min. The conversion i5 93~, the graft level 33.6 pph, the gra~t efficiency 89%
and the MFR 3.4 dg/min.
In E~ample 13, the reactor temperature is 90C, the initiator half-lives are 80 minutes and 20 minutes, respectively, the styrene feed rate is 1.01 pph/min, and the delay between peroxide and styrene additions is 10 minutes. The conversion is 98%, the graft level 35.1 pph, the graft efficiency 88%, and the MFR 7.5 dg~min.
S EYamDle lq The procedure and ingredients of Example 3 are used e~cept that the styrene feed level (1629 added) is 90.4 pph, the styrene addition rate is 1.14 pph/min, and the polypropylene used is Pro-fax 6501 having an IV of 2.5 dl/g, a MFR of 4.0 dg/min, a surface area (8.E.T) of 2.n m2/g, a pore volume fraction (by mercury porosimetry) o~
0.15, a weight average diameter of 0.2 mm, a bulk density of 0.53 g/ml, and a solubility in methylene chloride of 1.~
wt %. None of the pores in the particles are larger than 1 micron in diameter. The conversion is 93%, the graft level 31.0 pph, and the graft efficiency ~2%.
E~amPle 15 The procedure and ingredients of E~ample 3 are used e~cept that methyl methacrylate (29 pph) is used instead of styrene, the monomer/initiator mixture is added at a rate of 1.01 pph~min and the reactor temperature is ~5C. The amount of propylene homopolymer used is 4509, peroxy com-pound 4.5g, and methyl methecrylate 1359. The conversion is 86~, graft level 23.5 pph, and graft ef~iciency 90~.
ExamPle 16 The procedure and ingredients of E~ample 1 are used e~cept that methyl methacrylate (31.3 pph) is substituted for styrene, di(4-tert-butylcyclohe~yl)pero~y dicarbona~e (0.49 pph) is substituted for the pero~y ester, the amount of propylene homopolymer used is 4509, the reactor temper-ature is 70C, and the monomer is added at a rate of l.q pph/min. The conversion is 98%, the graft level 26.7 pph, the graft efficiency 85%, and the MFR 3.2 d~/min.
Example 17 The procedure and ingredients of Example 1 are used except that butyl acrylate (17.6 pph) is used instead of styrene and added at a rate of 1.17 pph/min (over 15 minutes), and 0.63 pph of the peroxy compound and a larger reactor are employed. The reactor is maintained at 105C
for 3 hours after all of the monomer had been added. A
vacuum then is applied at 104C for 1 hour followed by a 4-hour nitrogen purge at 120C. The conversion level is approximately 16.0 pph, the conversion 91%, and the MFR
10.4 dg/min.
~ample 18 The procedure and ingredients of Example 17 are used except that an ethylene/propylene random copolymer having an ethylene content of about 4.0% is substituted for the propylene homopolymer, and a mixture of styrene (4.42 pph and butyl acrylate (13.24 pph~ is used instead of butyl acrylate and added at a rate of 1.18 pph/min. (over 15 minutes). The pero~ide addition level is 0.5 pph, and the reactor temperature 100C. The four-hour nitrogen purge i5 at 100C. The conversion level for both monomers is 17.6 pph, the conversion 100%, and the MFR 9.7 dg/min.
~Yample 19 The procedure and ingredients of Example 17 are used e2cept that a chemically blended EPR-modified propylene homopolymer having a MFR of 4.89 dg/min, a polypropylene content of about 88%, and an EPR content of about 12%, wit~
an ethylene content of about 8%, is substituted for the propylene homopolymer, and styrene (53.8 pph) is substituted for the butyl acrylate. The styrene addit~on rate is 1.79 pph/min (30-minute addition period). The reactor temperature is 101C, and the peroxide addition level 0.2S pph. The nitrogen purge is conducted at 100C
for 5 hours. The conversion level is 45.5 pph, the conversion 85%, and the MFR 2.2 dg/min.
Example 20 The procedure and ingredients of Example 19 are used except that the EPR-modified propylene homopolymer used had a polypropylene content of 40~ and an EPR content of 60%, with an ethylene content of 39%, and a MFR of 16 dg/min.
The conversion level is 53.8 pph, the conversion 100~, and the MFR 2.1 dg/min.
Control ~periment 9 The procedure and ingredients of Example 17 are used with the following exceptions:
Pro-fax 6301 polypropylene having a MFR of 12.0 dg/min, a pore volume fraction of 0.15, and a weight average diameter of 0.2 mm is used instead o~ LBD-460A.
None of the pores in the particles are larger than 1 micron in diameter. The grafting monomer is n-butyl methacryla~e (17.1 pph), added at a rate of 0.56 pph/min (over a peri~d of 23 minutes). The initiator is tert-butyl-2-ethylhexyl-pero~y dicarbonate (1.3 pph), the reactor temperature is 135C., and the product is vacuum-dried at 135C for 5 hours. The conversion is 77%, and the MFR 152 dg/min.
E~ample 21 The procedure and ingredients of Example 1 are use~
e~cept that 1952g of propylene homopolymer is used instea~
of 400g, a 10 liter steel reactor is used instead of a 2 liter glass reactor, and the procedure was changed as se~
forth below.
The reactor is purged with nitrogen at room temperature until the active oxygen level reached 20 ppm and then heated to 120~C (+/- 1.5C) by circulating hot oil through the reactor jacket, and equilibrated to that tem-perature while nitrogen purging and stirring at 190 rpmcontinued. Styrene (12809), acrylonitrile (408.6g) and an oxygen-free mineral spirit solution of tert-butylperoxy 2-ethylhexanoate (78g o~ solution, 50% by weight of mineral s~irits) are added to a steel pressure cylinder and purged with nitrogen. The monomers/pero~ide mixture is fed to the reactor contents at a rate of 1.02 pph (parts per 100 parts polypropylene, by weight) per minute while maintaining the temperature of the reactor contents at 120~C (+/- 1.5C).
The total addition time is 85 minutes. The reactor is maintained at 120C with stirring for an additional 30 minutes following complete addition of the monomers. At the end of the grafting reaction period, a vacuum was drawn on the reactor contents and the temperature increased to 140C. The total heat up time under vacuum was 22.8 minutes. Once the temperature reached ls0C, the vacuum was broken with nitrogen and the contents purged with nitrogen for 30 minutes. After cool-down under a nitrogen blanket, the free-flowing solid product remaining in the reactor is discharged therefrom, dried, and weighed. Final weight of the product is 3597.7 grams, representing a conversion of 97.3%.
Other features, advantages and embodiments of the invention disclosed herein will be readily apparent to those e~ercising ordinary skill after reading the foregoin~
disclosures. In this regard, while specific embodiments ot the invention have been described in considerable detail, variations and modifications of these embodiments can be effected without departing from the spirit and scope o~ th~
invention as described and claimed.
Claims (26)
1. A method of making a polyolefin graft copolymer comprising, in a substantially non-oxidizing environment, (a) treating a particulate olefin polymer material at a temperature of about from 60° to 125°C with about from 0.1 to 6.0 pph of an organic compound which is a chemical free radical polymerization initiator and has a decomposition half-life at the temperature used of about from 1 to 240 minutes;
(b) treating said olefin polymer material at said temperature over a time period which coincides with or follows (a), with or without overlap, with about from 5 to 240 pph of at least one grafting monomer capable of being polymerized by free radicals, said monomer being added to said olefin polymer material over a time period sufficient to provide a rate of addition which does not exceed about 4.5 pph per minute at any addition level; and thereafter (c) removing any unreacted grafting monomer from the resultant grafted particulate olefin polymer material, and decomposing any unreacted initiator and deactivating any residual free radicals in said material.
(b) treating said olefin polymer material at said temperature over a time period which coincides with or follows (a), with or without overlap, with about from 5 to 240 pph of at least one grafting monomer capable of being polymerized by free radicals, said monomer being added to said olefin polymer material over a time period sufficient to provide a rate of addition which does not exceed about 4.5 pph per minute at any addition level; and thereafter (c) removing any unreacted grafting monomer from the resultant grafted particulate olefin polymer material, and decomposing any unreacted initiator and deactivating any residual free radicals in said material.
2. The method of Claim 1 wherein said grafting monomer is selected from the group consisting of vinyl-substituted aromatic, heterocyclic, and alicyclic compounds, unsaturated aliphatic carboxylic acids and derivatives thereof, unsaturated aliphatic nitriles, vinyl esters of aromatic and saturated aliphatic carboxylic acids, and mixtures thereof.
3. The method of Claim 1 wherein said olefin polymer material, after the addition of said monomer thereto, is maintained in contact with said monomer at the temperature employed for at least about 10 minutes.
4. The method of Claim 1 wherein in (c) said grafted olefin polymer material is maintained at a temperature ot at least about 110°C for at least about 5 minutes.
5. The method of Claim 1 wherein said organic compound is a peroxy compound.
6. The method of Claim 5 wherein more than about 40 pph of said grafting monomer is added to said olefin polymer material at a rate of about from 0.3 to 3.0 pph/minute.
7. The method of Claim 5 wherein said grafting monomer is added to said olefin polymer material over a time period which coincides with the period over which said peroxy compound is added thereto.
8. The method of Claim 5 wherein said grafting monomer is added to said olefin polymer material over a time period which follows the period over which said peroxy compound is added thereto.
9. The method of Claim 8 wherein the time period over which said grafting monomer is added to said olefin polymer material follows the time period over which said peroxy compound is added thereto after a delay of up to about 2.5 initiator half-lives.
10. The method of Claim 1 wherein said olefin polymer material is selected from the group consisting of an ethylene homopolymer, an ethylene copolymer, a propylene polymer material and a 1-butene homopolymer.
11. The method of Claim 10 wherein said olefin polymer material has (a) a pore volume fraction of at least about 0.07 wherein more than 40% of the pores have a Ulameter larger than 1 micron: (b) a surface area of at least 0.1 m2/g; and (c) a weight average diameter in the range of about from 0.4 to 7 mm.
12. The method of Claim 5 wherein said olefin polymer material is treated at a temperature of about from 80° to 120°C.
13. The method of Claim 6 wherein said organic peroxy compound is a peroxy ester or peroxy carbonate.
14. The method of Claim 13 wherein the half-life of said peroxy compound at the temperature employed is about from 5 to 100 minutes.
15. The method of Claim 5 wherein the amount of said peroxy compound with which said olefin polymer material is treated is about from 0.2 to 3 pph.
16. The method of Claim 5 wherein said grafting monomer is selected from the group consisting of styrene, alkyl-substituted styrenes, esters of acrylic and methacrylic acids, acrylonitrile and mixtures thereof.
17. The method of Claim 6 wherein said grafting monomer is selected from the group consisting of styrene alkyl-substituted styrenes, esters of acrylic and methacrylic acids, and mixtures thereof.
18. The method of Claim 6 wherein in (c) said grafted olefin polymer material is maintained at a temperature of at least 120°C for at least 20 minutes.
19. The method of Claim 5 wherein said grafting monomer is used neat.
20. The method of claim 5 wherein the grafting monomer is in solution.
21. The method of claim 3 wherein the decomposition half-life of the chemical free radical polymerization initiator at the temperature employed is about from 10 to 40 minutes.
22. The method of claim 1, 3, 4, 6, 7, 8, 9, 12 or 15, wherein the grafting monomer is selected from the group consisting of styrene, alkyl-substituted styrene, esters of acrylic and methacrylic acids, acrylonitrile and mixtures thereof, the organic compound is a peroxy compound having a decomposition half-life at the temperature used of from about 5 to 100 minutes, and the olefin polymer material is (A) a homo- or copolymer selected from the group consisting of an ethylene homopolymer having a density of 0.91 g/cm3 or greater, an ethylene random copolymer with up to 10% by weight of a C3 10 alpha-olefin having a density of 0.91 g/cm or greater, a propylene homopolymer, a propylene random copolymer with up to 10% by weight of ethylene or up to 20% by weight of C4 10 alpha-olefin and a 1-butene homopolymer, or (B) is the homo- or copolymer (A) which is impact-modified with from about 10 to about 60% by weight of (i) an ethylene-propylene rubber having an ethylene content of 7 to 70% by weight, (ii) an ethylene/butene-1 copolymer rubber having an ethylene content of from 30 to 70% by weight, (iii) a propylene/butene-l copolymer rubber having a butene-1 content of from 30 to 70% by weight, (iv) an ethylene/propylene/non-conjugated diene monomer rubber having an ethylene content of from 30 to 70% by weight and diene content of from 1 to 10% by weight or (v) an ethylene/propylene/butene terpolymer rubber having a propylene content of from 1 to 10% by weight and a butene content of from 30 to 70% by weight or a propylene content of from 30 to 70% by weight and a butene content of from 1 to 10%.
23. The method of claim 22 wherein the olefin polymer material has (a) a pore volume fraction of at least about 0.07 wherein more than 40% of the pores have a diameter larger than 1 micron; (b) a surface area of at least 0.1 m2/g; and (c) a weight average diameter in the range of about from 0.4 to 7 mm.
24. The method of claim 23 wherein the olefin polymer is a propylene homopolymer; and the grafting monomer is styrene, methyl methacrylate, acrylonitrile, 2-ethylhexyl acrylate, butyl acrylate or a mixture thereof.
25. The method of any one of claims 1 through 21 wherein the monomer is added to the olefin polymer material over a time period of from 5 minutes to 4 hours to provide the rate of addition of the step (b).
26. The method of claim 22 wherein the monomer is added to the olefin polymer material over a time period of from 5 minutes to 4 hours to provide the rate of addition of the step (b).
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US07/625,287 US5140074A (en) | 1990-01-26 | 1990-12-10 | Method of producing olefin polymer graft copolymers |
US07/625,287 | 1990-12-10 |
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CA2031406C (en) * | 1989-12-21 | 2002-05-28 | Paolo Galli | Graft copolymers of polyolefins and a method of producing same |
IL97430A0 (en) * | 1990-03-26 | 1992-06-21 | Himont Inc | Heat resistant propylene polymer compositions |
TW254949B (en) * | 1991-03-07 | 1995-08-21 | Himont Inc | |
IL102166A0 (en) * | 1991-06-21 | 1993-01-14 | Himont Inc | Grafting vinyl monomers on particulate olefin polymers |
US5397842A (en) * | 1991-08-20 | 1995-03-14 | Rohm And Haas Company | Polyolefin/segmented copolymer blend and process |
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-
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- 1990-12-10 US US07/625,287 patent/US5140074A/en not_active Expired - Lifetime
-
1991
- 1991-01-07 CA CA002033671A patent/CA2033671C/en not_active Expired - Fee Related
- 1991-01-07 IL IL96892A patent/IL96892A0/en unknown
- 1991-01-19 AT AT91100629T patent/ATE136313T1/en not_active IP Right Cessation
- 1991-01-19 DE DE69118418T patent/DE69118418T2/en not_active Expired - Fee Related
- 1991-01-19 DK DK91100629.4T patent/DK0439079T3/en active
- 1991-01-19 EP EP91100629A patent/EP0439079B1/en not_active Expired - Lifetime
- 1991-01-19 CN CN91100402A patent/CN1072232C/en not_active Expired - Fee Related
- 1991-01-22 FI FI910327A patent/FI910327L/en not_active Application Discontinuation
- 1991-01-23 HU HU91238A patent/HUT60301A/en unknown
- 1991-01-24 AU AU69955/91A patent/AU630539B2/en not_active Ceased
- 1991-01-24 KR KR1019910001164A patent/KR100191376B1/en not_active Expired - Fee Related
- 1991-01-24 YU YU11791A patent/YU11791A/en unknown
- 1991-01-24 NO NO91910285A patent/NO910285L/en unknown
- 1991-01-25 UA UA4894253A patent/UA37176C2/en unknown
- 1991-01-25 PT PT96576A patent/PT96576B/en not_active IP Right Cessation
- 1991-01-25 CZ CS91170A patent/CZ281368B6/en not_active IP Right Cessation
- 1991-01-25 JP JP3007703A patent/JP2980699B2/en not_active Expired - Lifetime
- 1991-01-25 BR BR919100336A patent/BR9100336A/en not_active IP Right Cessation
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DE69118418T2 (en) | 1996-09-12 |
ATE136313T1 (en) | 1996-04-15 |
KR910014418A (en) | 1991-08-31 |
CA2033671A1 (en) | 1991-07-27 |
DE69118418D1 (en) | 1996-05-09 |
CN1053614A (en) | 1991-08-07 |
PT96576A (en) | 1991-10-15 |
EP0439079B1 (en) | 1996-04-03 |
JP2980699B2 (en) | 1999-11-22 |
AU6995591A (en) | 1991-08-01 |
HUT60301A (en) | 1992-08-28 |
JPH04213313A (en) | 1992-08-04 |
CS9100170A2 (en) | 1991-09-15 |
DK0439079T3 (en) | 1996-05-06 |
US5140074A (en) | 1992-08-18 |
FI910327A7 (en) | 1991-07-27 |
KR100191376B1 (en) | 1999-06-15 |
HU910238D0 (en) | 1991-08-28 |
BR9100336A (en) | 1991-10-22 |
NO910285L (en) | 1991-07-29 |
FI910327L (en) | 1991-07-27 |
EP0439079A2 (en) | 1991-07-31 |
AU630539B2 (en) | 1992-10-29 |
EP0439079A3 (en) | 1991-11-13 |
CN1072232C (en) | 2001-10-03 |
NO910285D0 (en) | 1991-01-24 |
CZ281368B6 (en) | 1996-09-11 |
UA37176C2 (en) | 2001-05-15 |
IL96892A0 (en) | 1992-03-29 |
FI910327A0 (en) | 1991-01-22 |
YU11791A (en) | 1993-11-16 |
PT96576B (en) | 1998-07-31 |
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